WO2024027073A1 - Method and system for co-producing steam in power generation process - Google Patents

Method and system for co-producing steam in power generation process Download PDF

Info

Publication number
WO2024027073A1
WO2024027073A1 PCT/CN2022/138873 CN2022138873W WO2024027073A1 WO 2024027073 A1 WO2024027073 A1 WO 2024027073A1 CN 2022138873 W CN2022138873 W CN 2022138873W WO 2024027073 A1 WO2024027073 A1 WO 2024027073A1
Authority
WO
WIPO (PCT)
Prior art keywords
steam
heat exchanger
gas
cathode
oxygen
Prior art date
Application number
PCT/CN2022/138873
Other languages
French (fr)
Chinese (zh)
Inventor
李庆勋
王月
何盛宝
赵秦峰
钟海军
胡孝伟
赵晨欢
孟闪茹
李知春
Original Assignee
中国石油天然气股份有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 中国石油天然气股份有限公司 filed Critical 中国石油天然气股份有限公司
Publication of WO2024027073A1 publication Critical patent/WO2024027073A1/en

Links

Images

Classifications

    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22STEAM GENERATION
    • F22BMETHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00Methods of steam generation characterised by form of heating method
    • F22B1/02Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • HELECTRICITY
    • H01ELECTRIC ELEMENTS
    • H01MPROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00Fuel cells; Manufacture thereof
    • H01M8/04Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • HELECTRICITY
    • H01ELECTRIC ELEMENTS
    • H01MPROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00Fuel cells; Manufacture thereof
    • H01M8/04Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04067Heat exchange or temperature measuring elements, thermal insulation, e.g. heat pipes, heat pumps, fins
    • H01M8/04074Heat exchange unit structures specially adapted for fuel cell
    • HELECTRICITY
    • H01ELECTRIC ELEMENTS
    • H01MPROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00Fuel cells; Manufacture thereof
    • H01M8/04Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082Arrangements for control of reactant parameters, e.g. pressure or concentration
    • HELECTRICITY
    • H01ELECTRIC ELEMENTS
    • H01MPROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00Fuel cells; Manufacture thereof
    • H01M8/04Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04089Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
    • HELECTRICITY
    • H01ELECTRIC ELEMENTS
    • H01MPROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00Fuel cells; Manufacture thereof
    • H01M8/04Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04201Reactant storage and supply, e.g. means for feeding, pipes
    • HELECTRICITY
    • H01ELECTRIC ELEMENTS
    • H01MPROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00Fuel cells; Manufacture thereof
    • H01M8/06Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • HELECTRICITY
    • H01ELECTRIC ELEMENTS
    • H01MPROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00Fuel cells; Manufacture thereof
    • H01M8/06Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H01M8/0675Removal of sulfur
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30Hydrogen technology
    • Y02E60/50Fuel cells

Definitions

  • the present invention relates to the technical fields of energy development and energy conversion, and in particular to a method and system for co-generating steam in the power generation process.
  • steam is mainly produced directly by steam boilers.
  • Waste heat boilers are also one of the sources of steam.
  • most steam boilers use coal, residual oil, purge gas and refinery exhaust gas as raw materials in the production process, and use the combustion of the above raw materials to produce steam.
  • the purge gas and refinery exhaust gas during the production process can not only be used as fuel for steam production, but also can be directly used as fuel without reforming after removing sulfur and nitrogen impurities due to their high hydrogen content.
  • the solid oxide fuel cell anode provides fuel for power generation.
  • the solid oxide fuel cell is an all-solid-state power generation device that can efficiently convert hydrocarbon-containing fuels such as coal, oil, and natural gas into electrical energy. Its operating temperature is between 600 -1000°C, and its power generation process is not limited by the Carnot cycle. It can produce a large amount of high-temperature exhaust gas while generating power.
  • the high-temperature exhaust gas generated by solid oxide fuel cells contains a large amount of heat energy.
  • the existing technology is mainly used to co-produce hot water. If it can be used to co-produce steam, the waste heat quality can be significantly improved and carbon dioxide emissions during the steam production process can be significantly reduced.
  • the present invention is proposed to provide a method and system for co-generating steam in a power generation process that overcomes the above problems or at least partially solves the above problems.
  • embodiments of the present invention provide a system for co-generating steam in a power generation process, including: a fuel cell, a gas supply unit, an oxygen supply unit, and a first steam generation unit and/or a second steam generation unit;
  • the gas supply unit is connected to the anode of the fuel cell to provide fuel gas for the fuel cell;
  • the oxygen supply unit is connected to the cathode of the fuel cell to provide oxygen to the fuel cell;
  • the fuel cell is used to generate electricity using the fuel gas and the oxygen and produce anode exhaust gas and cathode exhaust gas;
  • a first steam generation unit connected to the anode, is used to generate steam by exchanging heat with water between the anode exhaust gas generated by the anode;
  • the second steam generation unit is connected to the cathode and is used to generate steam by exchanging heat with water between the cathode exhaust gas generated by the cathode.
  • the air supply unit includes: a purifier and an air supply preheating device
  • the purifier is used to treat impurities in the initial fuel gas
  • the air supply preheating device includes a first heat exchanger and a second heat exchanger, the first heat exchanger is connected to the purifier, and the second heat exchanger is connected to the fuel cell;
  • the gas supply preheating device is used to preheat the treated fuel gas so that the fuel gas reaches the first preset temperature and is supplied to the anode of the fuel cell.
  • the oxygen supply unit includes: a cathode exhaust gas storage tank, a compressor and an oxygen supply preheating device;
  • the cathode tail gas storage tank is connected to the second steam generation unit and is used to store the cathode tail gas and/or newly injected oxygen, and mix the cathode tail gas and the newly injected oxygen to obtain mixed oxygen, and the cathode tail gas is not yet reacting oxygen;
  • the compressor is connected to the cathode tail gas storage tank and is used to compress the cathode tail gas, newly injected oxygen or mixed oxygen to reach a preset pressure;
  • the oxygen supply preheating device is used to preheat the compressed cathode tail gas, newly injected oxygen or mixed oxygen to reach the second preset temperature.
  • the first steam generation unit includes a third heat exchanger and a fourth heat exchanger
  • the third heat exchanger is connected to the fuel cell anode to utilize anode exhaust gas and water to conduct The heat exchange produces the first medium-pressure steam
  • the fourth heat exchanger is connected to the third heat exchanger to use the anode tail gas and water to exchange heat to produce the first low-pressure steam
  • the second steam generation unit includes a fifth heat exchanger and a sixth heat exchanger.
  • the fifth heat exchanger is connected to the cathode of the fuel cell to generate second medium-pressure steam using cathode exhaust gas.
  • the sixth heat exchanger The heat exchanger is connected to the fifth heat exchanger to produce second low-pressure steam using the cathode exhaust gas.
  • system for co-generating steam in the power generation process also includes a third steam generation unit,
  • the third steam generation unit includes a positive gas tail gas burner, a seventh heat exchanger, an eighth heat exchanger and a ninth heat exchanger;
  • the positive gas tail gas burner is connected to the fourth heat exchanger for burning unreacted fuel gas in the anode tail gas to produce combustion products, and the positive gas tail gas burner is connected to an oxygen supply preheating device and a second heat exchanger.
  • the heater is connected to allow the combustion products to preheat the fuel gas and oxygen;
  • the seventh heat exchanger is connected to the second heat exchanger and the oxygen supply preheating device to produce third medium-pressure steam by exchanging heat between the preheated combustion products and water;
  • the eighth heat exchanger is connected to the seventh heat exchanger to utilize combustion products and water to exchange heat to produce third low-pressure steam;
  • the ninth heat exchanger is connected to the eighth heat exchanger to produce hot water and vent combustion products.
  • the eighth heat exchanger is connected to the first heat exchanger to preheat the fuel gas using third low-pressure steam.
  • an embodiment of the present invention also provides a method for co-generating steam in the power generation process using the above system.
  • the steps are as follows:
  • the gas supply unit provides fuel gas for the anode of the fuel cell, and the oxygen supply unit provides oxygen for the cathode of the fuel cell;
  • the first steam generation unit uses the anode tail gas and water to exchange heat to produce steam
  • the second steam generation unit uses the cathode tail gas and water to exchange heat to produce steam
  • the gas supply unit provides fuel gas for the anode of the fuel cell, including:
  • the gas supply unit purifies and preheats the initial fuel gas so that the fuel gas reaches a first preset temperature and is supplied to the anode of the fuel cell for reaction.
  • the oxygen supply unit provides oxygen for the cathode of the fuel cell, including:
  • the oxygen supply unit compresses and preheats the newly injected oxygen, the cathode tail gas, or the mixed oxygen of the newly injected oxygen and the cathode tail gas, so that it reaches the preset pressure and the second preset temperature, and then provides it to the fuel The reaction takes place at the cathode of the battery.
  • the first steam generation unit uses the anode tail gas and water to exchange heat to produce steam
  • the second steam generation unit uses the cathode tail gas and water to exchange heat to produce steam.
  • Steam including:
  • the first steam generation unit uses the anode tail gas to perform heat exchange in the third heat exchanger and the fourth heat exchanger to produce first medium pressure steam and first low pressure steam;
  • the second steam generation unit uses the cathode exhaust gas to perform heat exchange in the fifth heat exchanger and the sixth heat exchanger to produce second medium pressure steam and second low pressure steam.
  • the above method further includes:
  • the third steam generation unit uses the combustion products of the unreacted fuel gas to perform heat exchange in the seventh heat exchanger, the eighth heat exchanger and the ninth heat exchanger to produce third medium pressure steam, third Low pressure steam and hot water.
  • the third low-pressure steam preheats the fuel gas
  • the combustion products of the unreacted fuel gas are the fuel gas and the oxygen, which are preheated.
  • the hydrogen content of the initial fuel gas is not less than 30%;
  • the pressure of newly injected oxygen in the cathode tail gas storage tank is not higher than 4MPa;
  • the pressure is not higher than 2MPa.
  • the first preset temperature of the fuel gas entering the fuel cell anode after preheating is not lower than 700°C; after the anode exhaust gas produces the first medium-pressure steam, its temperature is not low At 400°C, after producing the first low-pressure steam, its temperature shall not be lower than 200°C.
  • the second preset temperature of the oxygen entering the fuel cell cathode after preheating is not lower than 700°C; after the cathode exhaust gas produces the second medium-pressure steam, the temperature is not lower than 400°C, After the second low-pressure steam is produced, the temperature shall not be lower than 150°C.
  • the method and system for co-generating steam in the power generation process use the fuel gas provided by the gas supply unit to the anode and the oxygen supply unit to provide oxygen to the cathode in the fuel cell for power generation reaction, and generate anode tail gas and cathode
  • the tail gas, the anode tail gas exchanges heat with water in the first steam generation unit to produce steam
  • the cathode tail gas exchanges heat with water in the second steam generation unit to produce steam, thereby realizing cogeneration of heat and power.
  • This co-generation steam method combines the power generation of fuel cells with the steam production process, using cheap resources such as industrial exhaust gas and refinery exhaust gas as fuel gas for the fuel cell to generate electricity, and then using the heat of the power generation exhaust gas to produce steam;
  • This fuel gas does not require a reforming reactor when used for fuel cell power generation, which is conducive to simplifying the reaction system, saving natural gas resources, and reducing investment costs; after using cheap resources such as industrial exhaust gas and refinery exhaust gas as fuel to generate electricity,
  • Using the heat generated by fuel cells to produce steam reduces the amount of carbon dioxide emissions in the process of burning raw materials to produce steam and reduces the cost of carbon emissions compared to directly using cheap resources such as industrial exhaust gas and refinery exhaust to produce steam. , make full use of the heat of power generation exhaust gas, improve the quality of waste heat of the fuel cell, save resources and reduce costs.
  • Figure 1 is a schematic structural diagram of a co-generation steam system in the power generation process in an embodiment of the present invention
  • FIG. 2 is a process flow diagram of the co-generation steam system in the embodiment of the present invention.
  • Figure 3 is a process flow diagram including a third steam generation unit in an embodiment of the present invention.
  • Figure 4 is a flow chart of a method for co-generating steam in a power generation process in an embodiment of the present invention.
  • 1-Purifier 2-First heat exchanger, 3-Second heat exchanger, 4-Fuel cell, 5-Third heat exchanger, 6-Fourth heat exchanger, 7-Anode tail gas burner, 8 -Oxygen supply preheating device, 9-fifth heat exchanger, 10-sixth heat exchanger, 11-cathode exhaust gas storage tank, 12-compressor, 13-seventh heat exchanger, 14-eighth heat exchanger , 15-ninth heat exchanger.
  • embodiments of the present invention provide a system and method for co-producing steam in the power generation process. To combine solid oxide fuel cells with steam production to increase the waste heat quality of solid oxide fuel cells.
  • SOFC solid oxide fuel cell
  • An embodiment of the present invention provides a system for co-generating steam during power generation, as shown in Figure 1 , including: a fuel cell 4, a gas supply unit 01, an oxygen supply unit 02, a first steam generation unit 03 and/or a Two steam generation units 05;
  • the gas supply unit 01 is connected to the anode of the fuel cell 4 to provide fuel gas for the fuel cell 4;
  • the oxygen supply unit 02 is connected to the cathode of the fuel cell 4 to provide oxygen to the fuel cell 4;
  • Fuel cell 4 is used to generate electricity using the above-mentioned fuel gas and oxygen and produce anode exhaust gas and cathode exhaust gas;
  • the first steam generation unit 03 is connected to the anode of the fuel cell and is used to generate steam by exchanging heat between the anode exhaust gas generated by the anode and water;
  • the second steam generation unit 05 is connected to the cathode of the fuel cell, and is used to generate steam by exchanging heat with water between the cathode exhaust gas generated by the cathode.
  • the above system combines the power generation of fuel cells with the process of steam production, uses cheap resources such as industrial exhaust gas and refinery exhaust gas as fuel gas for the fuel cell, and then uses the heat of the power generation exhaust gas to produce steam, which can make full use of resources. , compared with the process of burning raw materials to generate steam, it can reduce carbon dioxide emissions and reduce carbon emission costs. At the same time, it makes full use of the heat of the fuel cell power generation tail gas, avoids a large amount of waste of power generation waste heat, and improves the waste heat quality of the fuel cell. Resources can be saved and costs reduced.
  • the gas supply unit includes: purifier 1 and gas supply preheating device; purifier 1 is used to treat impurities in the initial fuel gas; initial fuel gases such as industrial purge gas and refinery exhaust gas have high hydrogen content, but contain sulfur and nitrogen. After the sulfur and nitrogen impurities are removed by the purifier 1, the impurities can be directly used as fuel gas to enter the fuel cell for power generation reaction without reforming.
  • the air supply preheating device includes at least one heat exchanger.
  • the air supply preheating device includes a first heat exchanger 2 and a second heat exchanger 3.
  • the first heat exchanger 2 is connected to the purifier 1
  • the second heat exchanger 3 is connected to the fuel cell 4;
  • the air supply preheating device is used to preheat the treated fuel gas, and the fuel purified by the purifier
  • the gas flows into the first heat exchanger 2 and the second heat exchanger 3 in sequence and undergoes two-stage heat exchange with the preheated material.
  • the fuel gas After the fuel gas reaches the first preset temperature, it is provided to the anode of the fuel cell 4 to preheat the gas.
  • the heat exchangers included in the device only need to enable the fuel gas to reach the first preset temperature when entering the fuel cell.
  • the present invention does not limit the number of specific heat exchangers.
  • the oxygen supply unit 02 of the embodiment of the present invention provides oxygen to the cathode of the fuel cell.
  • it can provide newly injected oxygen, or it can circulate unreacted oxygen at the cathode to the cathode or provide newly injected oxygen and unreacted oxygen at the cathode.
  • the mixed oxygen is supplied to the cathode.
  • the above-mentioned oxygen supply unit 02 includes: cathode tail gas storage tank 11, compressor 12 and oxygen supply preheating device 8;
  • the cathode exhaust gas storage tank 11 is connected to the second steam generation unit 05 for storing the cathode exhaust gas and/or newly injected oxygen, and mixing the cathode exhaust gas with the newly injected oxygen to obtain mixed oxygen.
  • the fuel cell The power generation reaction does not produce gas at the cathode, so the cathode exhaust gas is unreacted oxygen in the fuel cell 4;
  • the compressor 12 is connected to the cathode tail gas storage tank 11 and is used to compress the cathode tail gas, newly injected oxygen or mixed oxygen to reach a preset pressure; the oxygen supply preheating device 8 may include at least one heat exchanger for compressing The final cathode exhaust gas, newly injected oxygen or mixed oxygen are preheated to reach the second preset temperature.
  • the oxygen supply preheating device 8 includes a specific number of heat exchangers. The invention does not limit it, as long as It is sufficient that the cathode exhaust gas, newly injected oxygen or mixed oxygen can reach the second preset temperature when entering the fuel cell.
  • the above system can use exhaust gas from the anode and/or cathode of the fuel cell to generate steam. Therefore, the first steam generation unit 03 can be provided at the anode, the second steam generation unit 05 can be provided at the cathode, or both can be provided.
  • the first steam generation unit 03 may include at least one stage of heat exchanger. As shown in FIG. 2 , taking the first steam generation unit 03 including a two-stage heat exchanger as an example, the first steam generation unit 03 includes a third heat exchanger 5 and the fourth heat exchanger 6.
  • the third heat exchanger 5 is connected to the anode of the fuel cell 4 to use the anode exhaust gas and water to exchange heat to produce the first medium pressure steam.
  • the anode tail gas is connected to generate the first low-pressure steam by exchanging heat with water.
  • the anode tail gas includes water vapor, carbon dioxide and unreacted fuel gas generated by the fuel cell power generation reaction.
  • the waste heat of the anode tail gas is exchanged with water to generate the first low-pressure steam. Produce steam.
  • the second steam generation unit 05 may include at least one stage of heat exchanger.
  • the second steam generation unit 05 may include a two-stage heat exchanger.
  • the second steam generation unit 05 may include a fifth heat exchanger 9 and a sixth heat exchanger. 10.
  • the fifth heat exchanger 9 is connected to the cathode of the fuel cell 4 to use the cathode exhaust gas to exchange heat with the water flowing into the fifth heat exchanger to produce second medium-pressure steam.
  • the sixth heat exchanger 10 exchanges heat with the fifth heat exchanger.
  • the device 9 is connected to produce a second low-pressure steam by exchanging heat between the cathode exhaust gas and the water flowing into the sixth heat exchanger.
  • the unburned fuel gas in the anode exhaust gas can also be further used to generate steam.
  • the anode exhaust gas can also be used to generate steam.
  • the heat generated by the combustion of the unburned fuel gas preheats the fuel gas supplied to the anode of the fuel cell.
  • FIG 3. Another specific structural example of the above system is shown in Figure 3.
  • the system provided by the embodiment of the present invention also includes a third steam generation unit.
  • the third steam generation unit is connected to the first steam generation unit 03 and includes Yang gas tail gas burner 7 and at least one stage heat exchanger. Taking the third steam generation unit including a three-stage heat exchanger as an example, the third steam generation unit includes a seventh heat exchanger 13, an eighth heat exchanger 14 and a third heat exchanger.
  • the anode exhaust gas burner 7 is connected to the fourth heat exchanger 6 in the first steam generation unit 03 for burning the unreacted fuel gas in the anode exhaust gas to produce combustion products.
  • the anode exhaust gas burner 7 is connected to the oxygen supply preheating device. 8 is connected to the second heat exchanger 3 so that the combustion products of unreacted fuel gas can preheat the fuel gas entering the anode of the fuel cell and the oxygen entering the cathode of the fuel cell;
  • the seventh heat exchanger 13 is connected to the second heat exchanger 3 and the oxygen supply preheating device 8 to utilize the combustion products used to preheat the above-mentioned oxygen and fuel gas to pass into the seventh heat exchanger.
  • the water in the heat exchanger 13 performs heat exchange to produce the third medium-pressure steam;
  • the eighth heat exchanger 14 is connected to the seventh heat exchanger 13 to utilize the combustion products and water to perform heat exchange to produce the third low-pressure steam;
  • the ninth heat exchanger 15 is connected to the eighth heat exchanger 14 so that the combustion products after exchanging heat with the seventh heat exchanger 13 and the eighth heat exchanger 14 are passed into the ninth heat exchanger 15 to exchange heat with water. Produces hot water and vents combustion products.
  • the eighth heat exchanger 14 is connected to the first heat exchanger 2 to preheat the purified fuel gas using the third low-pressure steam produced in the eighth heat exchanger 14 .
  • the above system makes full use of the anode exhaust gas and cathode exhaust gas after fuel cell power generation to generate steam, and further utilizes the unburned fuel gas in the anode exhaust gas to generate steam, and establishes a cycle with the gas supply preheating device to provide fuel gas to the anode. Preheating, etc., through multiple cycles and utilization, the utilization rate of fuel gas can be further improved, the heat and exhaust gas generated in each link can be fully utilized, and the waste of resources can be avoided to the greatest extent.
  • an embodiment of the present invention also provides a method for co-producing steam using the system for co-producing steam in the power generation process. As shown in Figure 4, the steps are as follows:
  • Step S101 The gas supply unit provides fuel gas for the anode of the fuel cell, and the oxygen supply unit provides oxygen for the cathode of the fuel cell;
  • Step S102 Utilize fuel gas and oxygen to perform a power generation reaction in the fuel cell and generate anode exhaust gas and cathode exhaust gas;
  • Step S103 The first steam generation unit uses the anode exhaust gas and water to exchange heat to generate steam, and/or the second steam generation unit uses the cathode exhaust gas and water to exchange heat to generate steam.
  • step S101 the air supply unit provides fuel gas for the anode of the fuel cell, including: the air supply unit purifies and preheats the initial fuel gas, so that the fuel gas reaches the first preset temperature and is provided to the anode of the fuel cell for processing. reaction;
  • the oxygen supply unit provides oxygen to the cathode of the fuel cell and includes:
  • the oxygen supply unit compresses and preheats the newly injected oxygen, the cathode tail gas, or the mixed oxygen of the newly injected oxygen and the cathode tail gas, so that it reaches the preset pressure and the second preset temperature, and then provides it to the cathode of the fuel cell for processing. reaction.
  • the newly injected oxygen in the cathode tail gas storage tank can react with the oxygen by-product when electrolyzing water with renewable energy. This will help reduce energy loss and save energy costs.
  • step S103 the first steam generation unit uses the anode tail gas and water to exchange heat to produce steam, and/or the second steam generation unit uses the cathode tail gas and water to exchange heat to produce steam, including:
  • the first steam generation unit uses the anode tail gas to perform heat exchange in the third heat exchanger and the fourth heat exchanger to produce first medium pressure steam and first low pressure steam;
  • the second steam generation unit uses the cathode tail gas to perform heat exchange in the fifth heat exchanger.
  • the second medium-pressure steam and the second low-pressure steam are produced by heat exchange in the first steam generating unit and the sixth heat exchanger; optionally, in step 103, the first medium-pressure steam and/or the first medium-pressure steam can be produced only in the first steam generation unit.
  • the first low-pressure steam, the second medium-pressure steam and/or the second low-pressure steam can also be produced only in the second steam generation unit, or the steam can be produced in the first steam generation unit and the second steam generation unit at the same time .
  • the third steam generation unit connected to the first steam generation unit utilizes the combustion products of the unreacted fuel gas to perform heat exchange in the seventh heat exchanger, the eighth heat exchanger and the ninth heat exchanger to produce a third steam generation unit.
  • the third low-pressure steam is used to be connected to the first heat exchanger 2 to exchange heat between the purified fuel gas and the third low-pressure steam to preheat the purified fuel gas; after burning the unreacted fuel gas
  • the combustion products preheat the fuel gas entering the anode of the fuel cell and the oxygen entering the cathode of the fuel cell.
  • the hydrogen content of the initial fuel gas is not less than 30%; the newly injected oxygen content in the cathode tail gas storage tank
  • the pressure is not higher than 4MPa; after the cathode exhaust gas is pressurized by the compressor, the pressure is not higher than 2MPa; the first preset temperature of the fuel gas entering the fuel cell anode after preheating is not lower than 700°C; the first step in the production of the anode exhaust gas After compressing the steam, its temperature shall not be lower than 400°C. After producing the first low-pressure steam, its temperature shall not be lower than 200°C.
  • the second preset temperature of the oxygen entering the fuel cell cathode after preheating is not lower than 700°C; after the cathode tail gas produces the second medium-pressure steam, the temperature is not lower than 400°C; after the second low-pressure steam is produced, the temperature is not lower than 700°C. Below 150°C.
  • Example 1 When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 30%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 700°C, and the anode after reaction The exhaust gas temperature is 800°C.
  • the pressure of the newly injected fresh oxygen is 4MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 1.5MPa.
  • the temperature of the cathode reactants entering the solid fuel cell is 720°C, and the temperature of the cathode exhaust gas after the reaction is 820°C.
  • the temperature of the anode exhaust gas leaving the production medium-pressure steam heat exchanger is 500°C, and the temperature leaving the production low-pressure steam heat exchanger is 200°C.
  • the temperature of the cathode exhaust gas leaving the production medium-pressure steam heat exchanger is 500°C, and the temperature leaving the production low-pressure steam heat exchanger is 500°C.
  • the temperature of the unreacted fuel gas is 100°C when it leaves the hot water heat exchanger.
  • the production indicators are shown in Table 1.
  • the megawatt-level solid oxide fuel cell has generated a total of 8.55 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 4.275 million yuan, and co-produced 4,300 tons of medium-pressure steam and 4,180 tons of low-pressure steam, each calculated at 200 yuan / ton, 150 yuan / ton, the revenue is 860,000 yuan, 627,000 yuan, the total revenue is 5.762 million yuan, steam revenue accounts for 25.8%.
  • Example 2 When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 60%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 720°C, and the anode after reaction The exhaust gas temperature is 810°C. The pressure of the newly injected fresh oxygen is 3.5MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 2MPa. The temperature of the cathode reactants entering the solid oxide fuel cell is 700°C, and the temperature of the cathode exhaust gas after the reaction is 800°C.
  • hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas
  • the exhaust gas temperature is 810°C.
  • the pressure of the newly injected fresh oxygen is 3.5MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 2MPa.
  • the temperature of the anode tail gas leaving the production medium-pressure steam heat exchanger is 480°C
  • the temperature leaving the production low-pressure steam heat exchanger is 250°C
  • the temperature of the cathode tail gas leaving the production medium-pressure steam heat exchanger is 450°C
  • the unreacted fuel gas passes through the anode tail gas
  • the burner generates combustion products after combustion.
  • the temperature of the combustion products leaving the low-pressure steam heat exchanger is 180°C; the temperature leaving the hot water heat exchanger is 80°C.
  • the production indicators are shown in Table 2.
  • the megawatt-level solid oxide fuel cell has generated a total of 9.11 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 4.555 million yuan, and co-produced 4,030 tons of medium-pressure steam and 3,920 tons of low-pressure steam, each calculated at 200 yuan / ton, 150 yuan / ton, the revenue is 806,000 yuan, 588,000 yuan, the total revenue is 5.949 million yuan, steam revenue accounts for 23.4%.
  • Example 3 When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 100%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 710°C, and the anode after reaction The exhaust gas temperature is 820°C.
  • the pressure of the newly injected fresh oxygen is 3MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 1.8MPa.
  • the temperature of the cathode reactants entering the solid oxide fuel cell is 710°C, and the temperature of the cathode exhaust gas after the reaction is 810°C.
  • the temperature of the anode exhaust gas leaving the production medium-pressure steam heat exchanger is 400°C, and the temperature leaving the production low-pressure steam heat exchanger is 200°C.
  • the temperature of the cathode exhaust gas leaving the production medium-pressure steam heat exchanger is 400°C, and the temperature leaving the production low-pressure steam heat exchanger is 400°C.
  • the temperature of the unreacted fuel gas is 90°C when it leaves the hot water heat exchanger.
  • the production indicators are shown in Table 3.
  • the megawatt-level solid oxide fuel cell has generated a total of 10.25 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 5.125 million yuan, and co-produced 3,670 tons of medium-pressure steam and 3,530 tons of low-pressure steam, each calculated at 200 yuan / ton, 150 yuan / ton calculation, the revenue is 734,000 yuan, 530,000 yuan, the total revenue is 6.389 million yuan, steam revenue accounts for 19.8%.
  • Example 4 When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 20%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 680°C, and the anode after reaction The exhaust gas temperature is 780°C.
  • the pressure of the newly injected fresh oxygen is 4MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 1.8MPa.
  • the temperature of the cathode reactants entering the solid oxide fuel cell is 700°C, and the temperature of the cathode exhaust gas after the reaction is 770°C.
  • the temperature of the anode exhaust gas leaving the production medium-pressure steam heat exchanger is 380°C
  • the temperature leaving the production low-pressure steam heat exchanger is 200°C
  • the temperature of the cathode exhaust gas leaving the production medium-pressure steam heat exchanger is 400°C
  • the temperature leaving the production low-pressure steam heat exchanger is 400°C.
  • the temperature of the unreacted fuel gas is 90°C when it leaves the hot water heat exchanger.
  • the production indicators are shown in Table 4.
  • the megawatt-level solid oxide fuel cell has generated a total of 8.06 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 4.03 million yuan, and co-produced 4,420 tons of medium-pressure steam and 4,350 tons of low-pressure steam, respectively at 200 yuan / ton, 150 yuan / ton, the revenue is 884,000 yuan, 653,000 yuan, the total revenue is 5.567 million yuan, steam revenue accounts for 27.6%.
  • Example 5 When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 10%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 600°C, and the anode exhaust gas after reaction The temperature is 680°C.
  • the pressure of the newly injected fresh oxygen is 3MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 1.5MPa.
  • the temperature of the cathode reactants entering the solid oxide fuel cell is 600°C, and the temperature of the cathode exhaust gas after the reaction is 700°C.
  • the temperature of the anode exhaust gas leaving the production medium-pressure steam heat exchanger is 350°C, and the temperature leaving the production low-pressure steam heat exchanger is 160°C.
  • the temperature of the cathode exhaust gas leaving the production medium-pressure steam heat exchanger is 380°C, and the temperature leaving the production low-pressure steam heat exchanger is 380°C.
  • the temperature of the unreacted fuel gas is 95°C when it leaves the hot water heat exchanger.
  • the production indicators are shown in Table 5.
  • the megawatt solid oxide fuel cell has generated a total of 6.13 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 3.065 million yuan, and co-produced 4,815 tons of medium-pressure steam and 4,750 tons of low-pressure steam, each calculated at 200 yuan / ton, 150 yuan / ton, the revenue is 963,000 yuan, 713,000 yuan, the total revenue is 4.741 million yuan, steam revenue accounts for 35.4%.
  • the second preset temperature of the oxygen entering the fuel cell cathode after preheating is not lower than 700°C; after the cathode tail gas produces the second medium-pressure steam, the temperature is not lower than 400°C; after the second low-pressure steam is produced, the temperature is not lower than 700°C. below 150°C.
  • the total revenue generated by the cogeneration steam system's power generation and the total tonnage of medium-pressure steam and low-pressure steam produced is higher than the total revenue when fuel gas, oxygen and other related parameters are not within the preset range. Therefore, setting the relevant parameters of the process flow according to the range of fuel gas and oxygen related parameter setting requirements can better improve the efficiency of cogeneration and obtain better revenue effects.
  • the co-generation steam system in the power generation process of the embodiment of the present invention combines fuel cell combustion power generation with steam production. Compared with the traditional method of steam production through combustion, it reduces carbon dioxide emissions during the steam production process and simultaneously utilizes The anode exhaust gas and cathode exhaust gas of the fuel cell produce steam, which improves the waste heat quality of the anode exhaust gas and cathode exhaust gas and brings better economic benefits.

Landscapes

  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • General Chemical & Material Sciences (AREA)
  • Electrochemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Fuel Cell (AREA)

Abstract

A system for co-producing steam in a power generation process, which comprises a fuel cell, a gas supply unit, an oxygen supply unit, a first steam generation unit and/or a second steam generation unit. In the system, the fuel cell uses a fuel gas provided by the anode of the fuel cell and oxygen provided by the cathode of the fuel cell to carry out power generation reaction and produce an anode tail gas and a cathode tail gas. The anode tail gas exchanges heat with water at the first steam generation unit to generate steam, and the cathode tail gas exchanges heat with water at the second steam generation unit to generate steam, so as to realize heat-power co-production. The invention combines fuel cell power generation with the steam production process, utilizes cheap resources such as industrial purge gases and refinery tail gases as the fuel gases of the fuel cell for power generation, and then utilizes heat of the tail gas of power generation to produce steam, thereby improving the residual heat quality of the fuel cell and saving natural gas resources.

Description

一种发电过程中联产蒸汽的方法及系统A method and system for co-generating steam during power generation 技术领域Technical field
本发明涉及能源开发和能源转换技术领域,特别涉及一种发电过程中联产蒸汽的方法及系统。The present invention relates to the technical fields of energy development and energy conversion, and in particular to a method and system for co-generating steam in the power generation process.
背景技术Background technique
蒸汽作为炼油化工生产装置的重要动力和原料,主要由蒸汽锅炉直接生产,废热锅炉也是蒸汽的来源之一,蒸汽压力越高品质越高,也更适合作为动力使用。现有技术,为了降低蒸汽制造成本,蒸汽锅炉大多以煤炭、渣油以及生产过程中的驰放气、炼厂尾气为原料,利用以上原料的燃烧来生产蒸汽。而生产过程中的驰放气、炼厂尾气不但能作为生产蒸汽的燃料,且由于驰放气和炼厂尾气氢气含量高,脱除硫氮杂质后,不需重整也可直接作为燃料进入固体氧化物燃料电池阳极为发电提供燃料,固体氧化物燃料电池(SOFC)作为一种能将煤炭、石油、天然气等含碳氢燃料高效转化为电能的全固态发电装置,其工作温度介于600-1000℃,且其发电过程不受卡诺循环限制,在发电的同时能产生大量的高温尾气。As an important power and raw material for refining and chemical production equipment, steam is mainly produced directly by steam boilers. Waste heat boilers are also one of the sources of steam. The higher the steam pressure, the higher the quality and the more suitable it is for use as power. In the existing technology, in order to reduce the cost of steam manufacturing, most steam boilers use coal, residual oil, purge gas and refinery exhaust gas as raw materials in the production process, and use the combustion of the above raw materials to produce steam. The purge gas and refinery exhaust gas during the production process can not only be used as fuel for steam production, but also can be directly used as fuel without reforming after removing sulfur and nitrogen impurities due to their high hydrogen content. The solid oxide fuel cell anode provides fuel for power generation. The solid oxide fuel cell (SOFC) is an all-solid-state power generation device that can efficiently convert hydrocarbon-containing fuels such as coal, oil, and natural gas into electrical energy. Its operating temperature is between 600 -1000°C, and its power generation process is not limited by the Carnot cycle. It can produce a large amount of high-temperature exhaust gas while generating power.
发明内容Contents of the invention
本发明人发现,燃煤锅炉生产蒸汽时,二氧化碳排放强度大,碳排放处理成本高。而固体氧化物燃料电池产生的高温尾气含有大量热能,现有技术主要用于联产热水,如果能用于联产蒸汽,可显著提升余热品质,并能显著降低蒸汽生产过程中二氧化碳排放。The inventor found that when coal-fired boilers produce steam, the carbon dioxide emission intensity is high and the cost of carbon emission treatment is high. The high-temperature exhaust gas generated by solid oxide fuel cells contains a large amount of heat energy. The existing technology is mainly used to co-produce hot water. If it can be used to co-produce steam, the waste heat quality can be significantly improved and carbon dioxide emissions during the steam production process can be significantly reduced.
鉴于上述问题,提出了本发明以便提供一种克服上述问题或者至少部分地解决上述问题的一种发电过程联产蒸汽的方法及系统。In view of the above problems, the present invention is proposed to provide a method and system for co-generating steam in a power generation process that overcomes the above problems or at least partially solves the above problems.
第一方面,本发明实施例提供一种发电过程中联产蒸汽的系统,包括:燃料电池、供气单元、供氧单元、以及第一蒸汽生成单元和/或第二蒸汽生成单元;In a first aspect, embodiments of the present invention provide a system for co-generating steam in a power generation process, including: a fuel cell, a gas supply unit, an oxygen supply unit, and a first steam generation unit and/or a second steam generation unit;
所述供气单元,与所述燃料电池的阳极相连,以为所述燃料电池提供燃料气;The gas supply unit is connected to the anode of the fuel cell to provide fuel gas for the fuel cell;
所述供氧单元,与所述燃料电池的阴极相连,以为所述燃料电池提供氧气;The oxygen supply unit is connected to the cathode of the fuel cell to provide oxygen to the fuel cell;
所述燃料电池,用于使用所述燃料气和所述氧气发电并产生阳极尾气和阴极尾气;The fuel cell is used to generate electricity using the fuel gas and the oxygen and produce anode exhaust gas and cathode exhaust gas;
第一蒸汽生成单元,与所述阳极相连,用于利用所述阳极产生的阳极尾气与水进行换热产出蒸汽;A first steam generation unit, connected to the anode, is used to generate steam by exchanging heat with water between the anode exhaust gas generated by the anode;
第二蒸汽生成单元,与所述阴极相连,用于利用所述阴极产生的阴极尾气与水进行换热产出蒸汽。The second steam generation unit is connected to the cathode and is used to generate steam by exchanging heat with water between the cathode exhaust gas generated by the cathode.
在一些可选的实施例中,所述供气单元包括:净化器和供气预热装置;In some optional embodiments, the air supply unit includes: a purifier and an air supply preheating device;
所述净化器用于对初始燃料气的杂质处理;The purifier is used to treat impurities in the initial fuel gas;
所述供气预热装置包括第一换热器与第二换热器,所述第一换热器与所述净化器连接,所述第二换热器与所述燃料电池连接;所述供气预热装置用于对处理后的燃料气进行预热处理,使所述燃料气达到第一预设温度后提供到燃料电池的阳极。The air supply preheating device includes a first heat exchanger and a second heat exchanger, the first heat exchanger is connected to the purifier, and the second heat exchanger is connected to the fuel cell; The gas supply preheating device is used to preheat the treated fuel gas so that the fuel gas reaches the first preset temperature and is supplied to the anode of the fuel cell.
在一些可选的实施例中,所述供氧单元,包括:阴极尾气储罐、压缩机及供氧预热装置;In some optional embodiments, the oxygen supply unit includes: a cathode exhaust gas storage tank, a compressor and an oxygen supply preheating device;
所述阴极尾气储罐,与所述第二蒸汽生成单元相连,用于储存阴极尾气和/或新注入的氧气,并将阴极尾气与新注入的氧气混合得到混合氧气,所述阴极尾气为未反应的氧气;The cathode tail gas storage tank is connected to the second steam generation unit and is used to store the cathode tail gas and/or newly injected oxygen, and mix the cathode tail gas and the newly injected oxygen to obtain mixed oxygen, and the cathode tail gas is not yet reacting oxygen;
所述压缩机,与所述阴极尾气储罐相连,用于压缩阴极尾气、新注入的氧气或混合氧气使其达到预设压力;The compressor is connected to the cathode tail gas storage tank and is used to compress the cathode tail gas, newly injected oxygen or mixed oxygen to reach a preset pressure;
所述供氧预热装置用于对压缩后的阴极尾气、新注入的氧气或混合氧气进行预热使其达到第二预设温度。The oxygen supply preheating device is used to preheat the compressed cathode tail gas, newly injected oxygen or mixed oxygen to reach the second preset temperature.
在一些可选的实施例中,所述第一蒸汽生成单元包括第三换热器和第四换热器,所述第三换热器与所述燃料电池阳极相连以利用阳极尾气与水进行换热产出第一中压蒸汽,所述第四换热器与所述第三换热器相连以利用阳极尾气与水进行换热产出第一低压蒸汽;In some optional embodiments, the first steam generation unit includes a third heat exchanger and a fourth heat exchanger, and the third heat exchanger is connected to the fuel cell anode to utilize anode exhaust gas and water to conduct The heat exchange produces the first medium-pressure steam, and the fourth heat exchanger is connected to the third heat exchanger to use the anode tail gas and water to exchange heat to produce the first low-pressure steam;
所述第二蒸汽生成单元包括第五换热器与第六换热器,所述第五换热器与所述燃料电池阴极相连以利用阴极尾气产出第二中压蒸汽,所述第六换热器与所述第五换热器相连以利用阴极尾气产出第二低压蒸汽。The second steam generation unit includes a fifth heat exchanger and a sixth heat exchanger. The fifth heat exchanger is connected to the cathode of the fuel cell to generate second medium-pressure steam using cathode exhaust gas. The sixth heat exchanger The heat exchanger is connected to the fifth heat exchanger to produce second low-pressure steam using the cathode exhaust gas.
在一些可选的实施例中,所述发电过程中联产蒸汽的系统,还包括第三蒸汽生成单元,In some optional embodiments, the system for co-generating steam in the power generation process also includes a third steam generation unit,
所述第三蒸汽生成单元包括阳气尾气燃烧器、第七换热器、第八换热器及第九换热器;The third steam generation unit includes a positive gas tail gas burner, a seventh heat exchanger, an eighth heat exchanger and a ninth heat exchanger;
所述阳气尾气燃烧器与所述第四换热器相连用于燃烧阳极尾气中未反应的燃料气以产生燃烧产物,且所述阳气尾气燃烧器与供氧预热装置及第二换热器相连以使所述燃烧产物为所述燃料气及氧气预热;The positive gas tail gas burner is connected to the fourth heat exchanger for burning unreacted fuel gas in the anode tail gas to produce combustion products, and the positive gas tail gas burner is connected to an oxygen supply preheating device and a second heat exchanger. The heater is connected to allow the combustion products to preheat the fuel gas and oxygen;
所述第七换热器与所述第二换热器及供氧预热装置相连以利用用于预热后的所述燃烧产物与水换热生产第三中压蒸汽;The seventh heat exchanger is connected to the second heat exchanger and the oxygen supply preheating device to produce third medium-pressure steam by exchanging heat between the preheated combustion products and water;
所述第八换热器与所述第七换热器相连以利用燃烧产物与水进行换热生产第三低压蒸汽;The eighth heat exchanger is connected to the seventh heat exchanger to utilize combustion products and water to exchange heat to produce third low-pressure steam;
所述第九换热器与所述第八换热器相连以生产热水并放空燃烧产物。The ninth heat exchanger is connected to the eighth heat exchanger to produce hot water and vent combustion products.
在一些可选的实施例中,所述第八换热器与所述第一换热器相连,以利用第三低压蒸汽对所述燃料气进行预热。In some optional embodiments, the eighth heat exchanger is connected to the first heat exchanger to preheat the fuel gas using third low-pressure steam.
基于同一种发明构思,本发明实施例还提供一种利用上述系统进行发电过程中联产蒸汽的方法,其步骤如下:Based on the same inventive concept, an embodiment of the present invention also provides a method for co-generating steam in the power generation process using the above system. The steps are as follows:
供气单元为燃料电池的阳极提供燃料气,供氧单元为燃料电池的阴极提供氧气;The gas supply unit provides fuel gas for the anode of the fuel cell, and the oxygen supply unit provides oxygen for the cathode of the fuel cell;
利用所述燃料气与氧气在燃料电池中进行发电反应并产生阳极尾气和阴极尾气;Utilize the fuel gas and oxygen to perform a power generation reaction in a fuel cell and generate anode exhaust gas and cathode exhaust gas;
第一蒸汽生成单元利用所述阳极尾气与水进行换热产出蒸汽,和/或第二蒸汽生成单元利用所述阴极尾气与水进行换热产出蒸汽。The first steam generation unit uses the anode tail gas and water to exchange heat to produce steam, and/or the second steam generation unit uses the cathode tail gas and water to exchange heat to produce steam.
在一些可选的实施例中,所述供气单元为所述燃料电池的阳极提供燃料气,包括:In some optional embodiments, the gas supply unit provides fuel gas for the anode of the fuel cell, including:
所述供气单元对初始燃料气进行净化处理并预热,使所述燃料气达到第一预设温度后提供给燃料电池的阳极进行反应。The gas supply unit purifies and preheats the initial fuel gas so that the fuel gas reaches a first preset temperature and is supplied to the anode of the fuel cell for reaction.
在一些可选的实施例中,所述供氧单元为所述燃料电池的阴极提供氧气,包括:In some optional embodiments, the oxygen supply unit provides oxygen for the cathode of the fuel cell, including:
所述供氧单元将新注入的氧气、阴极尾气、或新注入的氧气和阴极尾气的混合氧气进行压缩和预热,使其达到预设压力和第二预设温度后,提供给所述燃料电池的阴极进行反应。The oxygen supply unit compresses and preheats the newly injected oxygen, the cathode tail gas, or the mixed oxygen of the newly injected oxygen and the cathode tail gas, so that it reaches the preset pressure and the second preset temperature, and then provides it to the fuel The reaction takes place at the cathode of the battery.
在一些可选的实施例中,所述第一蒸汽生成单元利用所述阳极尾气与水进行换热产出蒸汽,和/或第二蒸汽生成单元利用所述阴极尾气与水进行换热产出蒸汽,包括:In some optional embodiments, the first steam generation unit uses the anode tail gas and water to exchange heat to produce steam, and/or the second steam generation unit uses the cathode tail gas and water to exchange heat to produce steam. Steam, including:
所述第一蒸汽生成单元利用所述阳极尾气在第三换热器及第四换热器内进行换热产出第一中压蒸汽和第一低压蒸汽;The first steam generation unit uses the anode tail gas to perform heat exchange in the third heat exchanger and the fourth heat exchanger to produce first medium pressure steam and first low pressure steam;
所述第二蒸汽生成单元利用所述阴极尾气在第五换热器及第六换热器内进行换热产出第二中压蒸汽和第二低压蒸汽。The second steam generation unit uses the cathode exhaust gas to perform heat exchange in the fifth heat exchanger and the sixth heat exchanger to produce second medium pressure steam and second low pressure steam.
在一些可选的实施例中,上述方法还包括:In some optional embodiments, the above method further includes:
所述第三蒸汽生成单元利用未反应的燃料气燃烧后的燃烧产物在第七换热器、第八换热器及第九换热器内进行换热产出第三中压蒸汽、第三低压蒸汽和热水。The third steam generation unit uses the combustion products of the unreacted fuel gas to perform heat exchange in the seventh heat exchanger, the eighth heat exchanger and the ninth heat exchanger to produce third medium pressure steam, third Low pressure steam and hot water.
在一些可选的实施例中,所述第三低压蒸汽为所述燃料气进行预热;In some optional embodiments, the third low-pressure steam preheats the fuel gas;
所述未反应的燃料气燃烧后的产物为所述燃料气及所述氧气进行预热。The combustion products of the unreacted fuel gas are the fuel gas and the oxygen, which are preheated.
在一些可选的实施例中,所述初始燃料气氢气含量不低于30%;In some optional embodiments, the hydrogen content of the initial fuel gas is not less than 30%;
所述阴极尾气储罐中新注入的氧气的压力不高于4MPa;The pressure of newly injected oxygen in the cathode tail gas storage tank is not higher than 4MPa;
所述阴极尾气经压缩机增压后,压力不高于2MPa。After the cathode exhaust gas is pressurized by the compressor, the pressure is not higher than 2MPa.
在一些可选的实施例中,所述燃料气经过预热进入所述燃料电池阳极的第一预设温度不低于700℃;所述阳极尾气生产第一中压蒸汽后,其温度不低于400℃,生产第一低压蒸汽后,其温度不低于200℃。In some optional embodiments, the first preset temperature of the fuel gas entering the fuel cell anode after preheating is not lower than 700°C; after the anode exhaust gas produces the first medium-pressure steam, its temperature is not low At 400℃, after producing the first low-pressure steam, its temperature shall not be lower than 200℃.
在一些可选的实施例中,所述氧气经过预热进入所述燃料电池阴极的第二预设温度不低于700℃;阴极尾气生产第二中压蒸汽后,温度不低于400℃,生产第二低压蒸汽后,温度不低于150℃。In some optional embodiments, the second preset temperature of the oxygen entering the fuel cell cathode after preheating is not lower than 700°C; after the cathode exhaust gas produces the second medium-pressure steam, the temperature is not lower than 400°C, After the second low-pressure steam is produced, the temperature shall not be lower than 150°C.
本发明实施例提供的上述技术方案的有益效果至少包括:The beneficial effects of the above technical solutions provided by the embodiments of the present invention at least include:
本发明实施例提供的发电过程联产蒸汽的方法及系统,在燃料电池内利用供气单元为其阳极提供的燃料气与供氧单元为其阴极提供氧气进行发电反应,并产生阳极尾气和阴极尾气,阳极尾气在第一蒸汽生成单元与水进行换热产出蒸汽,阴极尾气在第二蒸汽生成单元与水进行换热产出蒸汽,进而实现热电联供。该联产蒸汽的方法,将燃料电池的发电与蒸汽生产的过程相结合,利用工业弛放气、炼厂尾气等廉价资源作为燃料电池的燃料气发电后再利用发电尾气的热量产出蒸汽;该燃料气用于燃料电池的发电时不需重整反应器,有利于简化反应系统、节省天然气资源,降低了投资成本;利用工业弛放气、炼厂尾气等廉价资源作为燃料发电后,再利用燃料电池产生的热量产出蒸汽,相比于直接使用工业弛放气、炼厂尾气等廉价资源产出蒸汽而言,减少了原料燃烧产生蒸汽过程中二氧化碳的排放量,降低了碳排放成本,充分利用发电尾气的热量,提高了燃料电池的余热品质,节约资源并降低成本。The method and system for co-generating steam in the power generation process provided by the embodiments of the present invention use the fuel gas provided by the gas supply unit to the anode and the oxygen supply unit to provide oxygen to the cathode in the fuel cell for power generation reaction, and generate anode tail gas and cathode The tail gas, the anode tail gas exchanges heat with water in the first steam generation unit to produce steam, and the cathode tail gas exchanges heat with water in the second steam generation unit to produce steam, thereby realizing cogeneration of heat and power. This co-generation steam method combines the power generation of fuel cells with the steam production process, using cheap resources such as industrial exhaust gas and refinery exhaust gas as fuel gas for the fuel cell to generate electricity, and then using the heat of the power generation exhaust gas to produce steam; This fuel gas does not require a reforming reactor when used for fuel cell power generation, which is conducive to simplifying the reaction system, saving natural gas resources, and reducing investment costs; after using cheap resources such as industrial exhaust gas and refinery exhaust gas as fuel to generate electricity, Using the heat generated by fuel cells to produce steam reduces the amount of carbon dioxide emissions in the process of burning raw materials to produce steam and reduces the cost of carbon emissions compared to directly using cheap resources such as industrial exhaust gas and refinery exhaust to produce steam. , make full use of the heat of power generation exhaust gas, improve the quality of waste heat of the fuel cell, save resources and reduce costs.
本发明的其它特征和优点将在随后的说明书中阐述,并且,部分地从说明书中变得显而易见,或者通过实施本发明而了解。本发明的目的和其他优点可通过在所写的说明书、权利要求书、以及附图中所特别指出的结构来实现和获得。Additional features and advantages of the invention will be set forth in the description which follows, and in part will be apparent from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention may be realized and attained by the structure particularly pointed out in the written description and claims hereof as well as the appended drawings.
下面通过附图和实施例,对本发明的技术方案做进一步的详细描述。The technical solution of the present invention will be further described in detail below through the accompanying drawings and examples.
附图说明Description of the drawings
附图用来提供对本发明的进一步理解,并且构成说明书的一部分,与本发明的实施例一起用于解释本发明,并不构成对本发明的限制。在附图中:The drawings are used to provide a further understanding of the present invention and constitute a part of the specification. They are used to explain the present invention together with the embodiments of the present invention and do not constitute a limitation of the present invention. In the attached picture:
图1为本发明实施例中发电过程联产蒸汽系统的结构示意图;Figure 1 is a schematic structural diagram of a co-generation steam system in the power generation process in an embodiment of the present invention;
图2为本发明实施例中联产蒸汽系统工艺流程图;Figure 2 is a process flow diagram of the co-generation steam system in the embodiment of the present invention;
图3为本发明实施例中包含第三蒸汽生成单元的工艺流程图;Figure 3 is a process flow diagram including a third steam generation unit in an embodiment of the present invention;
图4为本发明实施例中发电过程联产蒸汽方法的流程图。Figure 4 is a flow chart of a method for co-generating steam in a power generation process in an embodiment of the present invention.
附图标记:Reference signs:
1-净化器,2-第一换热器,3-第二换热器,4-燃料电池,5-第三换热器,6-第四换热器,7-阳极尾气燃烧器,8-供氧预热装置,9-第五换热器,10-第六换热器,11-阴极尾气储罐,12-压缩机,13-第七换热器,14-第八换热器,15-第九换热器。1-Purifier, 2-First heat exchanger, 3-Second heat exchanger, 4-Fuel cell, 5-Third heat exchanger, 6-Fourth heat exchanger, 7-Anode tail gas burner, 8 -Oxygen supply preheating device, 9-fifth heat exchanger, 10-sixth heat exchanger, 11-cathode exhaust gas storage tank, 12-compressor, 13-seventh heat exchanger, 14-eighth heat exchanger , 15-ninth heat exchanger.
具体实施方式Detailed ways
下面将参照附图更详细地描述本公开的示例性实施例。虽然附图中显示了本公开的示例性实施例,然而应当理解,可以以各种形式实现本公开而不应被这里阐述的实施例所限制。相反,提供这些实施例是为了能够更透彻地理解本公开,并且能够将本公开的范围完整的传达给本领域的技术人员。Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. Although exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be implemented in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided to provide a thorough understanding of the disclosure, and to fully convey the scope of the disclosure to those skilled in the art.
为了解决现有蒸汽生产的过程中,二氧化碳排放量大,同时固体氧化物燃料电池(SOFC)余热品质不高的问题,本发明实施例提供了一种发电过程中联产蒸汽的系统及方法,以将固体氧化物燃料电池与蒸汽生产相结合,以增加固体氧化燃料电池的余热品质。In order to solve the problems of large carbon dioxide emissions and low quality of solid oxide fuel cell (SOFC) waste heat in the existing steam production process, embodiments of the present invention provide a system and method for co-producing steam in the power generation process. To combine solid oxide fuel cells with steam production to increase the waste heat quality of solid oxide fuel cells.
本发明实施例提供的一种发电过程中联产蒸汽的系统,如图1所示,包括:燃料电池4、供气单元01、供氧单元02、以及第一蒸汽生成单元03和/或第二蒸汽生成单元05;An embodiment of the present invention provides a system for co-generating steam during power generation, as shown in Figure 1 , including: a fuel cell 4, a gas supply unit 01, an oxygen supply unit 02, a first steam generation unit 03 and/or a Two steam generation units 05;
其中,供气单元01与燃料电池4的阳极相连,以为燃料电池4提供燃料气;Among them, the gas supply unit 01 is connected to the anode of the fuel cell 4 to provide fuel gas for the fuel cell 4;
供氧单元02与燃料电池4的阴极相连,以为燃料电池4提供氧气;The oxygen supply unit 02 is connected to the cathode of the fuel cell 4 to provide oxygen to the fuel cell 4;
燃料电池4,用于使用上述燃料气和氧气发电并产生阳极尾气和阴极尾气; Fuel cell 4 is used to generate electricity using the above-mentioned fuel gas and oxygen and produce anode exhaust gas and cathode exhaust gas;
第一蒸汽生成单元03,与燃料电池阳极相连,用于利用阳极产生的阳极尾气与水进行换热产出蒸汽;The first steam generation unit 03 is connected to the anode of the fuel cell and is used to generate steam by exchanging heat between the anode exhaust gas generated by the anode and water;
第二蒸汽生成单元05,与燃料电池阴极相连,用于利用阴极产生的阴极尾气与水进行换热产出蒸汽。The second steam generation unit 05 is connected to the cathode of the fuel cell, and is used to generate steam by exchanging heat with water between the cathode exhaust gas generated by the cathode.
上述系统,将燃料电池的发电与蒸汽生产的过程相结合,利用工业弛放气、炼厂尾气等廉价资源作为燃料电池的燃料气发电后再利用发电尾气的热量产出蒸汽,可以充分利用资源,相对于原料燃烧产生蒸汽过程而言,可以减少二氧化碳的排放量,降低了碳排放成本,同时充分利用了燃料电池发电尾气的热量,避免发电余热的大量浪费,提高了燃料电池的余热品质,可以节约资源并降低成本。The above system combines the power generation of fuel cells with the process of steam production, uses cheap resources such as industrial exhaust gas and refinery exhaust gas as fuel gas for the fuel cell, and then uses the heat of the power generation exhaust gas to produce steam, which can make full use of resources. , compared with the process of burning raw materials to generate steam, it can reduce carbon dioxide emissions and reduce carbon emission costs. At the same time, it makes full use of the heat of the fuel cell power generation tail gas, avoids a large amount of waste of power generation waste heat, and improves the waste heat quality of the fuel cell. Resources can be saved and costs reduced.
在一些可选的实施例中,上述系统的一种具体结构示例如图2所示。In some optional embodiments, a specific structural example of the above system is shown in Figure 2.
供气单元包括:净化器1和供气预热装置;净化器1用于对初始燃料气的杂质处理; 工业驰放气、炼厂尾气等初始燃料气氢气含量高,但其内含有硫氮杂质,经过净化器1脱除硫氮杂质后,无需重整可直接作为燃料气进入燃料电池内进行发电反应。The gas supply unit includes: purifier 1 and gas supply preheating device; purifier 1 is used to treat impurities in the initial fuel gas; initial fuel gases such as industrial purge gas and refinery exhaust gas have high hydrogen content, but contain sulfur and nitrogen. After the sulfur and nitrogen impurities are removed by the purifier 1, the impurities can be directly used as fuel gas to enter the fuel cell for power generation reaction without reforming.
可选的,供气预热装置包括至少一个换热器,如图2所示的以两个换热器为例,供气预热装置包括第一换热器2与第二换热器3,第一换热器2与净化器1连接,第二换热器3与燃料电池4连接;供气预热装置用于对处理后的燃料气进行预热处理,经净化器净化后的燃料气依次通入第一换热器2与第二换热器3中经过与预热物料进行两级换热,使燃料气达到第一预设温度后提供到燃料电池4阳极,供气预热装置中包括的换热器只需使燃料气进入燃料电池时能达到第一预设温度即可,对于具体换热器的个数,本发明不作限定。Optionally, the air supply preheating device includes at least one heat exchanger. As shown in Figure 2, taking two heat exchangers as an example, the air supply preheating device includes a first heat exchanger 2 and a second heat exchanger 3. , the first heat exchanger 2 is connected to the purifier 1, and the second heat exchanger 3 is connected to the fuel cell 4; the air supply preheating device is used to preheat the treated fuel gas, and the fuel purified by the purifier The gas flows into the first heat exchanger 2 and the second heat exchanger 3 in sequence and undergoes two-stage heat exchange with the preheated material. After the fuel gas reaches the first preset temperature, it is provided to the anode of the fuel cell 4 to preheat the gas. The heat exchangers included in the device only need to enable the fuel gas to reach the first preset temperature when entering the fuel cell. The present invention does not limit the number of specific heat exchangers.
本发明实施例的供氧单元02为燃料电池的阴极提供氧气,可选的,可以提供新注入的氧气,也可以将阴极未反应氧气循环提供给阴极或提供新注入的氧气与阴极未反应氧气的混合氧气给阴极,上述供氧单元02,包括:阴极尾气储罐11、压缩机12及供氧预热装置8;The oxygen supply unit 02 of the embodiment of the present invention provides oxygen to the cathode of the fuel cell. Optionally, it can provide newly injected oxygen, or it can circulate unreacted oxygen at the cathode to the cathode or provide newly injected oxygen and unreacted oxygen at the cathode. The mixed oxygen is supplied to the cathode. The above-mentioned oxygen supply unit 02 includes: cathode tail gas storage tank 11, compressor 12 and oxygen supply preheating device 8;
阴极尾气储罐11与第二蒸汽生成单元05连接,用于储存阴极尾气和/或新注入的氧气,并将阴极尾气与新注入的氧气混合得到混合氧气,在本发明实施例中,燃料电池的发电反应在阴极不产生气体,因此阴极尾气为燃料电池4内未反应的氧气;The cathode exhaust gas storage tank 11 is connected to the second steam generation unit 05 for storing the cathode exhaust gas and/or newly injected oxygen, and mixing the cathode exhaust gas with the newly injected oxygen to obtain mixed oxygen. In the embodiment of the present invention, the fuel cell The power generation reaction does not produce gas at the cathode, so the cathode exhaust gas is unreacted oxygen in the fuel cell 4;
压缩机12与阴极尾气储罐11相连,用于压缩阴极尾气、新注入的氧气或混合氧气使其达到预设压力;供氧预热装置8可包含至少一个换热器,以用于对压缩后的阴极尾气、新注入的氧气或混合氧气进行预热使其达到第二预设温度,可选的,对于供氧预热装置8包含换热器具体个数,本发明不作限定,只需使阴极尾气、新注入的氧气或混合氧气进入燃料电池时能达到第二预设温度即可。The compressor 12 is connected to the cathode tail gas storage tank 11 and is used to compress the cathode tail gas, newly injected oxygen or mixed oxygen to reach a preset pressure; the oxygen supply preheating device 8 may include at least one heat exchanger for compressing The final cathode exhaust gas, newly injected oxygen or mixed oxygen are preheated to reach the second preset temperature. Optionally, the oxygen supply preheating device 8 includes a specific number of heat exchangers. The invention does not limit it, as long as It is sufficient that the cathode exhaust gas, newly injected oxygen or mixed oxygen can reach the second preset temperature when entering the fuel cell.
上述系统,可以利用燃料电池阳极和/或阴极的尾气来产生蒸汽,因此,可以在阳极设置第一蒸汽生成单元03,可以在阴极设置第二蒸汽生成单元05,也可以两者都设置。The above system can use exhaust gas from the anode and/or cathode of the fuel cell to generate steam. Therefore, the first steam generation unit 03 can be provided at the anode, the second steam generation unit 05 can be provided at the cathode, or both can be provided.
第一蒸汽生成单元03可以包括至少一级换热器,如图2所示,以第一蒸汽生成单元03包括两级换热器为例,第一蒸汽生成单元03包括第三换热器5和第四换热器6,第三换热器5与燃料电池4阳极相连以利用阳极尾气与水进行换热产出第一中压蒸汽,第四换热器6与第三换热器5相连以利用阳极尾气与水进行换热产出第一低压蒸汽,上述阳极尾气包括燃料电池发电反应产生的水蒸汽、二氧化碳及未反应完的燃料气,利用阳极尾气的余热与水的热交换来产出蒸汽。The first steam generation unit 03 may include at least one stage of heat exchanger. As shown in FIG. 2 , taking the first steam generation unit 03 including a two-stage heat exchanger as an example, the first steam generation unit 03 includes a third heat exchanger 5 and the fourth heat exchanger 6. The third heat exchanger 5 is connected to the anode of the fuel cell 4 to use the anode exhaust gas and water to exchange heat to produce the first medium pressure steam. The fourth heat exchanger 6 and the third heat exchanger 5 The anode tail gas is connected to generate the first low-pressure steam by exchanging heat with water. The anode tail gas includes water vapor, carbon dioxide and unreacted fuel gas generated by the fuel cell power generation reaction. The waste heat of the anode tail gas is exchanged with water to generate the first low-pressure steam. Produce steam.
第二蒸汽生成单元05可以包括至少一级换热器,以第二蒸汽生成单元05包括两级 换热器为例,第二蒸汽生成单元05包括第五换热器9与第六换热器10,第五换热器9与燃料电池4阴极相连以利用阴极尾气与通入第五换热器的水进行换热产出第二中压蒸汽,第六换热器10与第五换热器9相连以利用阴极尾气与通入第六换热器的水进行换热产出第二低压蒸汽。The second steam generation unit 05 may include at least one stage of heat exchanger. For example, the second steam generation unit 05 may include a two-stage heat exchanger. The second steam generation unit 05 may include a fifth heat exchanger 9 and a sixth heat exchanger. 10. The fifth heat exchanger 9 is connected to the cathode of the fuel cell 4 to use the cathode exhaust gas to exchange heat with the water flowing into the fifth heat exchanger to produce second medium-pressure steam. The sixth heat exchanger 10 exchanges heat with the fifth heat exchanger. The device 9 is connected to produce a second low-pressure steam by exchanging heat between the cathode exhaust gas and the water flowing into the sixth heat exchanger.
在一些可选的实施例中,除了利用阳极尾气、阴极尾气的热量通过换热的方式产出蒸汽外,还可以进一步利用阳极尾气中未燃烧的燃料气来产出蒸汽,也可以利用阳极尾气中未燃烧的燃料气燃烧后产生的热量为提供给燃料电池阳极的燃料气进行预热。可选地,上述系统的另一种具体结构示例如图3所示,本发明实施例提供的系统还包括第三蒸汽生成单元,第三蒸汽生成单元与第一蒸汽生成单元03相连,其包括阳气尾气燃烧器7和至少一级换热器,以第三蒸汽生成单元包括三级换热器为例,第三蒸汽生成单元包括第七换热器13、第八换热器14及第九换热器15;In some optional embodiments, in addition to using the heat of the anode exhaust gas and the cathode exhaust gas to generate steam through heat exchange, the unburned fuel gas in the anode exhaust gas can also be further used to generate steam. The anode exhaust gas can also be used to generate steam. The heat generated by the combustion of the unburned fuel gas preheats the fuel gas supplied to the anode of the fuel cell. Optionally, another specific structural example of the above system is shown in Figure 3. The system provided by the embodiment of the present invention also includes a third steam generation unit. The third steam generation unit is connected to the first steam generation unit 03 and includes Yang gas tail gas burner 7 and at least one stage heat exchanger. Taking the third steam generation unit including a three-stage heat exchanger as an example, the third steam generation unit includes a seventh heat exchanger 13, an eighth heat exchanger 14 and a third heat exchanger. Nine heat exchangers 15;
其中阳气尾气燃烧器7与第一蒸汽生成单元03中第四换热器6相连用于燃烧阳极尾气中未反应的燃料气以产生燃烧产物,阳气尾气燃烧器7与供氧预热装置8及第二换热器3相连以使未反应的燃料气的燃烧产物为进入燃料电池阳极的燃料气及进入燃料电池阴极的氧气进行预热;The anode exhaust gas burner 7 is connected to the fourth heat exchanger 6 in the first steam generation unit 03 for burning the unreacted fuel gas in the anode exhaust gas to produce combustion products. The anode exhaust gas burner 7 is connected to the oxygen supply preheating device. 8 is connected to the second heat exchanger 3 so that the combustion products of unreacted fuel gas can preheat the fuel gas entering the anode of the fuel cell and the oxygen entering the cathode of the fuel cell;
如图3所示,第七换热器13与第二换热器3及供氧预热装置8相连以利用用于给上述氧气及燃料气预热后的燃烧产物与通入第七换热器13的水进行换热产第三中压蒸汽;第八换热器14与第七换热器13相连以利用燃烧产物与水进行换热生产第三低压蒸汽;As shown in Figure 3, the seventh heat exchanger 13 is connected to the second heat exchanger 3 and the oxygen supply preheating device 8 to utilize the combustion products used to preheat the above-mentioned oxygen and fuel gas to pass into the seventh heat exchanger. The water in the heat exchanger 13 performs heat exchange to produce the third medium-pressure steam; the eighth heat exchanger 14 is connected to the seventh heat exchanger 13 to utilize the combustion products and water to perform heat exchange to produce the third low-pressure steam;
第九换热器15与第八换热器14相连以使与第七换热器13及第八换热器14换热后的燃烧产物通入第九换热器15中与水进行换热生产热水并放空燃烧产物。The ninth heat exchanger 15 is connected to the eighth heat exchanger 14 so that the combustion products after exchanging heat with the seventh heat exchanger 13 and the eighth heat exchanger 14 are passed into the ninth heat exchanger 15 to exchange heat with water. Produces hot water and vents combustion products.
在第三蒸汽生成单元中,第八换热器14与第一换热器2相连,以利用在第八换热器14中产出的第三低压蒸汽对净化后的燃料气进行预热。In the third steam generation unit, the eighth heat exchanger 14 is connected to the first heat exchanger 2 to preheat the purified fuel gas using the third low-pressure steam produced in the eighth heat exchanger 14 .
上述系统,充分利用燃料电池发电后的阳极尾气、阴极尾气产生蒸汽的同时,进一步利用阳极尾气中未燃烧的燃料气产生蒸汽,以及与供气预热装置建立循环,为提供给阳极的燃料气进行预热等等,通过多重循环和利用,使燃料气的利用率进一步提高,充分利用各个环节产生的热量和尾气,最大程度的避免资源浪费。The above system makes full use of the anode exhaust gas and cathode exhaust gas after fuel cell power generation to generate steam, and further utilizes the unburned fuel gas in the anode exhaust gas to generate steam, and establishes a cycle with the gas supply preheating device to provide fuel gas to the anode. Preheating, etc., through multiple cycles and utilization, the utilization rate of fuel gas can be further improved, the heat and exhaust gas generated in each link can be fully utilized, and the waste of resources can be avoided to the greatest extent.
基于同一种发明构思,本发明实施例还提供一种利用上述发电过程中联产蒸汽的系统进行联产蒸汽的方法,如图4所示,其步骤如下:Based on the same inventive concept, an embodiment of the present invention also provides a method for co-producing steam using the system for co-producing steam in the power generation process. As shown in Figure 4, the steps are as follows:
步骤S101:供气单元为燃料电池的阳极提供燃料气,供氧单元为燃料电池的阴极 提供氧气;Step S101: The gas supply unit provides fuel gas for the anode of the fuel cell, and the oxygen supply unit provides oxygen for the cathode of the fuel cell;
步骤S102:利用燃料气与氧气在燃料电池中进行发电反应并产生阳极尾气和阴极尾气;Step S102: Utilize fuel gas and oxygen to perform a power generation reaction in the fuel cell and generate anode exhaust gas and cathode exhaust gas;
步骤S103:第一蒸汽生成单元利用阳极尾气与水进行换热产出蒸汽,和/或第二蒸汽生成单元利用阴极尾气与水进行换热产出蒸汽。Step S103: The first steam generation unit uses the anode exhaust gas and water to exchange heat to generate steam, and/or the second steam generation unit uses the cathode exhaust gas and water to exchange heat to generate steam.
在步骤S101中,供气单元为燃料电池的阳极提供燃料气,包括:供气单元对初始燃料气进行净化处理并预热,使燃料气达到第一预设温度后提供给燃料电池的阳极进行反应;In step S101, the air supply unit provides fuel gas for the anode of the fuel cell, including: the air supply unit purifies and preheats the initial fuel gas, so that the fuel gas reaches the first preset temperature and is provided to the anode of the fuel cell for processing. reaction;
供氧单元为燃料电池的阴极提供氧气,包括:The oxygen supply unit provides oxygen to the cathode of the fuel cell and includes:
供氧单元将新注入的氧气、阴极尾气、或新注入的氧气和阴极尾气的混合氧气进行压缩和预热,使其达到预设压力和第二预设温度后,提供给燃料电池的阴极进行反应。随着可再生能源装机容量的增大,电解水装置逐渐增加会带来更多的副产氧气,阴极尾气储罐内新注入的氧气可利用可再生能源电解水时副产的氧气进行反应,从而有利于降低能量的损耗,节约能源成本。The oxygen supply unit compresses and preheats the newly injected oxygen, the cathode tail gas, or the mixed oxygen of the newly injected oxygen and the cathode tail gas, so that it reaches the preset pressure and the second preset temperature, and then provides it to the cathode of the fuel cell for processing. reaction. As the installed capacity of renewable energy increases, the gradual increase in water electrolysis devices will bring more by-product oxygen. The newly injected oxygen in the cathode tail gas storage tank can react with the oxygen by-product when electrolyzing water with renewable energy. This will help reduce energy loss and save energy costs.
在步骤S103中,第一蒸汽生成单元利用阳极尾气与水进行换热产出蒸汽,和/或第二蒸汽生成单元利用阴极尾气与水进行换热产出蒸汽,包括:In step S103, the first steam generation unit uses the anode tail gas and water to exchange heat to produce steam, and/or the second steam generation unit uses the cathode tail gas and water to exchange heat to produce steam, including:
第一蒸汽生成单元利用阳极尾气在第三换热器及第四换热器内进行换热产出第一中压蒸汽和第一低压蒸汽;第二蒸汽生成单元利用阴极尾气在第五换热器及第六换热器内进行换热产出第二中压蒸汽和第二低压蒸汽;可选的,在步骤103中,可只在第一蒸汽生成单元中生产第一中压蒸汽和/或第一低压蒸汽,也可只在第二蒸汽生成单元中生产第二中压蒸汽和/或第二低压蒸汽,也可同时在第一蒸汽生成单元和第二蒸汽生成单元中进行蒸汽的生产。The first steam generation unit uses the anode tail gas to perform heat exchange in the third heat exchanger and the fourth heat exchanger to produce first medium pressure steam and first low pressure steam; the second steam generation unit uses the cathode tail gas to perform heat exchange in the fifth heat exchanger. The second medium-pressure steam and the second low-pressure steam are produced by heat exchange in the first steam generating unit and the sixth heat exchanger; optionally, in step 103, the first medium-pressure steam and/or the first medium-pressure steam can be produced only in the first steam generation unit. Or the first low-pressure steam, the second medium-pressure steam and/or the second low-pressure steam can also be produced only in the second steam generation unit, or the steam can be produced in the first steam generation unit and the second steam generation unit at the same time .
可选的,本发明实施例中利用如图3所示的结构示例进行联产蒸汽时还包括:Optionally, in the embodiment of the present invention, when the structural example shown in Figure 3 is used for co-generation of steam, it also includes:
与第一蒸汽生成单元相连的第三蒸汽生成单元利用未反应的燃料气燃烧后的燃烧产物在第七换热器、第八换热器及第九换热器内进行换热产出第三中压蒸汽、第三低压蒸汽和热水。The third steam generation unit connected to the first steam generation unit utilizes the combustion products of the unreacted fuel gas to perform heat exchange in the seventh heat exchanger, the eighth heat exchanger and the ninth heat exchanger to produce a third steam generation unit. Medium pressure steam, third low pressure steam and hot water.
其中第三低压蒸汽用于与第一换热器2相连,以使净化后的燃料气与第三低压蒸汽进行换热,以对净化后的燃料气进行预热;未反应的燃料气燃烧后的燃烧产物为进入燃料电池阳极的燃料气及进入燃料电池阴极的氧气进行预热。The third low-pressure steam is used to be connected to the first heat exchanger 2 to exchange heat between the purified fuel gas and the third low-pressure steam to preheat the purified fuel gas; after burning the unreacted fuel gas The combustion products preheat the fuel gas entering the anode of the fuel cell and the oxygen entering the cathode of the fuel cell.
对于发电过程中联产蒸汽方法的具体执行过程,已在相关的联产蒸汽系统的实施例 中进行详细描述,此处将不做详细阐述说明。The specific implementation process of the co-generation steam method in the power generation process has been described in detail in the relevant embodiments of the co-generation steam system, and will not be described in detail here.
在进行固体氧化物燃料电池发电并联产蒸汽的过程中,对燃料气及氧气的相关参数设置有以下要求:初始燃料气氢气含量不低于30%;阴极尾气储罐中新注入的氧气的压力不高于4MPa;阴极尾气经压缩机增压后,压力不高于2MPa;燃料气经过预热进入燃料电池阳极的第一预设温度不低于700℃;所述阳极尾气生产第一中压蒸汽后,其温度不低于400℃,生产第一低压蒸汽后,其温度不低于200℃。所述氧气经过预热进入所述燃料电池阴极的第二预设温度不低于700℃;阴极尾气生产第二中压蒸汽后,温度不低于400℃,生产第二低压蒸汽后,温度不低于150℃。In the process of solid oxide fuel cell power generation and co-generation of steam, the following requirements are set for the relevant parameters of fuel gas and oxygen: the hydrogen content of the initial fuel gas is not less than 30%; the newly injected oxygen content in the cathode tail gas storage tank The pressure is not higher than 4MPa; after the cathode exhaust gas is pressurized by the compressor, the pressure is not higher than 2MPa; the first preset temperature of the fuel gas entering the fuel cell anode after preheating is not lower than 700°C; the first step in the production of the anode exhaust gas After compressing the steam, its temperature shall not be lower than 400°C. After producing the first low-pressure steam, its temperature shall not be lower than 200°C. The second preset temperature of the oxygen entering the fuel cell cathode after preheating is not lower than 700°C; after the cathode tail gas produces the second medium-pressure steam, the temperature is not lower than 400°C; after the second low-pressure steam is produced, the temperature is not lower than 700°C. Below 150℃.
针对不同的燃料气及氧气的参数,如图3所示,对上述发电过程联产蒸汽的工艺流程进行举例说明如下:According to different parameters of fuel gas and oxygen, as shown in Figure 3, the process flow of co-generation of steam in the above power generation process is explained as follows:
示例1:当工业驰放气、炼厂尾气等含氢气燃料气氢气含量为30%,燃料气经净化处理和预热后进入固体氧化物燃料电池SOFC阳极的温度为700℃,反应后的阳极尾气温度为800℃。新注入的新鲜氧气压力为4MPa,进入阴极尾气储罐的阴极尾气经增压机增压,压力为1.5MPa。进入固体燃料电池的阴极反应物温度为720℃,反应后的阴极尾气温度为820℃。阳极尾气离开生产中压蒸汽换热器温度为500℃,离开生产低压蒸汽换热器温度为200℃,阴极尾气离开生产中压蒸汽换热器温度为500℃,离开生产低压蒸汽换热器温度为200℃;未反应的燃料气经阳极尾气燃烧器燃烧后生成燃烧产物,其燃烧产物离开生产热水换热器的温度为100℃。生产指标见表1。按照8760小时/年核算,兆瓦级固体氧化物燃料电池累计发电855万度,按0.5元/度计算,收入427.5万元,联产中压蒸汽4300吨、低压蒸汽4180吨,分别按照200元/吨、150元/吨计算,收入为86万元、62.7万元,总收入576.2万元,蒸汽收入占比25.8%。Example 1: When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 30%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 700°C, and the anode after reaction The exhaust gas temperature is 800°C. The pressure of the newly injected fresh oxygen is 4MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 1.5MPa. The temperature of the cathode reactants entering the solid fuel cell is 720°C, and the temperature of the cathode exhaust gas after the reaction is 820°C. The temperature of the anode exhaust gas leaving the production medium-pressure steam heat exchanger is 500°C, and the temperature leaving the production low-pressure steam heat exchanger is 200°C. The temperature of the cathode exhaust gas leaving the production medium-pressure steam heat exchanger is 500°C, and the temperature leaving the production low-pressure steam heat exchanger is 500°C. The temperature of the unreacted fuel gas is 100℃ when it leaves the hot water heat exchanger. The production indicators are shown in Table 1. Calculated based on 8,760 hours/year, the megawatt-level solid oxide fuel cell has generated a total of 8.55 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 4.275 million yuan, and co-produced 4,300 tons of medium-pressure steam and 4,180 tons of low-pressure steam, each calculated at 200 yuan / ton, 150 yuan / ton, the revenue is 860,000 yuan, 627,000 yuan, the total revenue is 5.762 million yuan, steam revenue accounts for 25.8%.
表1 工业驰放气、炼厂尾气等含氢气燃料气进气量2MW(低热值)生产指标值Table 1 Production index value of hydrogen-containing fuel gas intake volume 2MW (low calorific value) such as industrial exhaust gas and refinery exhaust gas
Figure PCTCN2022138873-appb-000001
Figure PCTCN2022138873-appb-000001
示例2:当工业驰放气、炼厂尾气等含氢气燃料气氢气含量为60%,燃料气经净化处理和预热后进入固体氧化物燃料电池SOFC阳极的温度为720℃,反应后的阳极尾气温度为810℃。新注入的新鲜氧气压力为3.5MPa,进入阴极尾气储罐的阴极尾气经增压机增压,压力为2MPa。进入固体氧化物燃料电池的阴极反应物温度为700℃,反应后 的阴极尾气温度为800℃。阳极尾气离开生产中压蒸汽换热器温度为480℃,离开生产低压蒸汽换热器温度为250℃,阴极尾气离开生产中压蒸汽换热器温度为450℃,未反应的燃料气经阳极尾气燃烧器燃烧后生成燃烧产物,其燃烧产物离开生产低压蒸汽换热器温度为180℃;离开生产热水换热器的温度为80℃。生产指标见表2。按照8760小时/年核算,兆瓦级固体氧化物燃料电池累计发电911万度,按0.5元/度计算,收入455.5万元,联产中压蒸汽4030吨、低压蒸汽3920吨,分别按照200元/吨、150元/吨计算,收入为80.6万元、58.8万元,总收入594.9万元,蒸汽收入占比23.4%。Example 2: When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 60%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 720°C, and the anode after reaction The exhaust gas temperature is 810°C. The pressure of the newly injected fresh oxygen is 3.5MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 2MPa. The temperature of the cathode reactants entering the solid oxide fuel cell is 700°C, and the temperature of the cathode exhaust gas after the reaction is 800°C. The temperature of the anode tail gas leaving the production medium-pressure steam heat exchanger is 480°C, the temperature leaving the production low-pressure steam heat exchanger is 250°C, the temperature of the cathode tail gas leaving the production medium-pressure steam heat exchanger is 450°C, and the unreacted fuel gas passes through the anode tail gas The burner generates combustion products after combustion. The temperature of the combustion products leaving the low-pressure steam heat exchanger is 180°C; the temperature leaving the hot water heat exchanger is 80°C. The production indicators are shown in Table 2. Calculated based on 8,760 hours/year, the megawatt-level solid oxide fuel cell has generated a total of 9.11 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 4.555 million yuan, and co-produced 4,030 tons of medium-pressure steam and 3,920 tons of low-pressure steam, each calculated at 200 yuan / ton, 150 yuan / ton, the revenue is 806,000 yuan, 588,000 yuan, the total revenue is 5.949 million yuan, steam revenue accounts for 23.4%.
表2 工业驰放气、炼厂尾气等含氢气燃料气进气量2MW(低热值)生产指标值Table 2 Production index value of hydrogen-containing fuel gas intake volume 2MW (low calorific value) such as industrial exhaust gas and refinery exhaust gas
Figure PCTCN2022138873-appb-000002
Figure PCTCN2022138873-appb-000002
示例3:当工业驰放气、炼厂尾气等含氢气燃料气氢气含量为100%,燃料气经净化处理和预热后进入固体氧化物燃料电池SOFC阳极的温度为710℃,反应后的阳极尾气温度为820℃。新注入的新鲜氧气压力为3MPa,进入阴极尾气储罐的阴极尾气经增压机增压,压力为1.8MPa。进入固体氧化物燃料电池的阴极反应物温度为710℃,反应后的阴极尾气温度为810℃。阳极尾气离开生产中压蒸汽换热器温度为400℃,离开生产低压蒸汽换热器温度为200℃,阴极尾气离开生产中压蒸汽换热器温度为400℃,离开生产低压蒸汽换热器温度为150℃;未反应的燃料气经阳极尾气燃烧器燃烧后生成燃烧产物,其燃烧产物离开生产热水换热器的温度为90℃。生产指标见表3。按照8760小时/年核算,兆瓦级固体氧化物燃料电池累计发电1025万度,按0.5元/度计算,收入512.5万元,联产中压蒸汽3670吨、低压蒸汽3530吨,分别按照200元/吨、150元/吨计算,收入为73.4万元、53.0万元,总收入638.9万元,蒸汽收入占比19.8%。Example 3: When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 100%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 710°C, and the anode after reaction The exhaust gas temperature is 820°C. The pressure of the newly injected fresh oxygen is 3MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 1.8MPa. The temperature of the cathode reactants entering the solid oxide fuel cell is 710°C, and the temperature of the cathode exhaust gas after the reaction is 810°C. The temperature of the anode exhaust gas leaving the production medium-pressure steam heat exchanger is 400°C, and the temperature leaving the production low-pressure steam heat exchanger is 200°C. The temperature of the cathode exhaust gas leaving the production medium-pressure steam heat exchanger is 400°C, and the temperature leaving the production low-pressure steam heat exchanger is 400°C. The temperature of the unreacted fuel gas is 90℃ when it leaves the hot water heat exchanger. The production indicators are shown in Table 3. Calculated based on 8,760 hours/year, the megawatt-level solid oxide fuel cell has generated a total of 10.25 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 5.125 million yuan, and co-produced 3,670 tons of medium-pressure steam and 3,530 tons of low-pressure steam, each calculated at 200 yuan / ton, 150 yuan / ton calculation, the revenue is 734,000 yuan, 530,000 yuan, the total revenue is 6.389 million yuan, steam revenue accounts for 19.8%.
表3 工业驰放气、炼厂尾气等含氢气燃料气进气量2MW(低热值)生产指标值Table 3 Production index values of 2MW (low calorific value) hydrogen-containing fuel gas intake such as industrial exhaust gas and refinery exhaust gas
Figure PCTCN2022138873-appb-000003
Figure PCTCN2022138873-appb-000003
示例4:当工业驰放气、炼厂尾气等含氢气燃料气氢气含量为20%,燃料气经净化 处理和预热后进入固体氧化物燃料电池SOFC阳极的温度为680℃,反应后的阳极尾气温度为780℃。新注入的新鲜氧气压力为4MPa,进入阴极尾气储罐的阴极尾气经增压机增压,压力为1.8MPa。进入固体氧化物燃料电池的阴极反应物温度为700℃,反应后的阴极尾气温度为770℃。阳极尾气离开生产中压蒸汽换热器温度为380℃,离开生产低压蒸汽换热器温度为200℃,阴极尾气离开生产中压蒸汽换热器温度为400℃,离开生产低压蒸汽换热器温度为150℃;未反应的燃料气经阳极尾气燃烧器燃烧后生成燃烧产物,其燃烧产物离开生产热水换热器温度为90℃。生产指标见表4。按照8760小时/年核算,兆瓦级固体氧化物燃料电池累计发电806万度,按0.5元/度计算,收入403万元,联产中压蒸汽4420吨、低压蒸汽4350吨,分别按照200元/吨、150元/吨计算,收入为88.4万元、65.3万元,总收入556.7万元,蒸汽收入占比27.6%。Example 4: When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 20%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 680°C, and the anode after reaction The exhaust gas temperature is 780°C. The pressure of the newly injected fresh oxygen is 4MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 1.8MPa. The temperature of the cathode reactants entering the solid oxide fuel cell is 700°C, and the temperature of the cathode exhaust gas after the reaction is 770°C. The temperature of the anode exhaust gas leaving the production medium-pressure steam heat exchanger is 380°C, the temperature leaving the production low-pressure steam heat exchanger is 200°C, the temperature of the cathode exhaust gas leaving the production medium-pressure steam heat exchanger is 400°C, and the temperature leaving the production low-pressure steam heat exchanger is 400°C. The temperature of the unreacted fuel gas is 90℃ when it leaves the hot water heat exchanger. The production indicators are shown in Table 4. Calculated based on 8,760 hours/year, the megawatt-level solid oxide fuel cell has generated a total of 8.06 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 4.03 million yuan, and co-produced 4,420 tons of medium-pressure steam and 4,350 tons of low-pressure steam, respectively at 200 yuan / ton, 150 yuan / ton, the revenue is 884,000 yuan, 653,000 yuan, the total revenue is 5.567 million yuan, steam revenue accounts for 27.6%.
表4 工业驰放气、炼厂尾气等含氢气燃料气进气量2MW(低热值)生产指标值Table 4 Production index value of 2MW (low calorific value) hydrogen-containing fuel gas intake such as industrial exhaust gas and refinery exhaust gas
Figure PCTCN2022138873-appb-000004
Figure PCTCN2022138873-appb-000004
示例5:当工业驰放气、炼厂尾气等含氢气燃料气氢气含量10%,燃料气经净化处理和预热后进入固体氧化物燃料电池SOFC阳极的温度为600℃,反应后的阳极尾气温度为680℃。新注入的新鲜氧气压力为3MPa,进入阴极尾气储罐的阴极尾气经增压机增压,压力为1.5MPa。进入固体氧化物燃料电池的阴极反应物温度为600℃,反应后的阴极尾气温度为700℃。阳极尾气离开生产中压蒸汽换热器温度为350℃,离开生产低压蒸汽换热器温度为160℃,阴极尾气离开生产中压蒸汽换热器温度为380℃,离开生产低压蒸汽换热器温度为180℃;未反应的燃料气经阳极尾气燃烧器燃烧后生成燃烧产物,其燃烧产物离开生产热水换热器的温度为95℃。生产指标见表5。按照8760小时/年核算,兆瓦级固体氧化物燃料电池累计发电613万度,按0.5元/度计算,收入306.5万元,联产中压蒸汽4815吨、低压蒸汽4750吨,分别按照200元/吨、150元/吨计算,收入为96.3万元、71.3万元,总收入474.1万元,蒸汽收入占比35.4%。Example 5: When the hydrogen content of hydrogen-containing fuel gas such as industrial exhaust gas and refinery exhaust gas is 10%, the temperature of the fuel gas entering the solid oxide fuel cell SOFC anode after purification and preheating is 600°C, and the anode exhaust gas after reaction The temperature is 680℃. The pressure of the newly injected fresh oxygen is 3MPa, and the cathode exhaust gas entering the cathode exhaust gas storage tank is pressurized by the supercharger to a pressure of 1.5MPa. The temperature of the cathode reactants entering the solid oxide fuel cell is 600°C, and the temperature of the cathode exhaust gas after the reaction is 700°C. The temperature of the anode exhaust gas leaving the production medium-pressure steam heat exchanger is 350°C, and the temperature leaving the production low-pressure steam heat exchanger is 160°C. The temperature of the cathode exhaust gas leaving the production medium-pressure steam heat exchanger is 380°C, and the temperature leaving the production low-pressure steam heat exchanger is 380°C. The temperature of the unreacted fuel gas is 95℃ when it leaves the hot water heat exchanger. The production indicators are shown in Table 5. Calculated based on 8,760 hours/year, the megawatt solid oxide fuel cell has generated a total of 6.13 million kilowatt-hours of electricity, calculated at 0.5 yuan/degree, with an income of 3.065 million yuan, and co-produced 4,815 tons of medium-pressure steam and 4,750 tons of low-pressure steam, each calculated at 200 yuan / ton, 150 yuan / ton, the revenue is 963,000 yuan, 713,000 yuan, the total revenue is 4.741 million yuan, steam revenue accounts for 35.4%.
表5 工业驰放气、炼厂尾气等含氢气燃料气进气量2MW(低热值)生产指标值Table 5 Production index value of 2MW (low calorific value) hydrogen-containing fuel gas intake such as industrial exhaust gas and refinery exhaust gas
Figure PCTCN2022138873-appb-000005
Figure PCTCN2022138873-appb-000005
Figure PCTCN2022138873-appb-000006
Figure PCTCN2022138873-appb-000006
综合示例1至示例5所示可以看出:联产蒸汽的整个过程中,当初始燃料气氢气含量不低于30%;阴极尾气储罐中新注入的氧气的压力不高于4MPa;阴极尾气经压缩机增压后,压力不高于2MPa;燃料气经过预热进入所述燃料电池阳极的第一预设温度不低于700℃;所述阳极尾气生产第一中压蒸汽后,其温度不低于400℃,生产第一低压蒸汽后,其温度不低于200℃。所述氧气经过预热进入所述燃料电池阴极的第二预设温度不低于700℃;阴极尾气生产第二中压蒸汽后,温度不低于400℃,生产第二低压蒸汽后,温度不低于150℃时。整个发电过程中联产蒸汽系统发电度数及生产中压蒸汽和低压蒸汽总吨数带来的总收入要高于燃料气、氧气等相关参数不在预设范围内时的总收入。因此根据燃料气及氧气相关参数设置要求的范围进行该工艺流程相关参数的设置,能更好的提高热电联产的效率,获得更好的收益效果。It can be seen from the comprehensive examples 1 to 5 that: during the entire process of co-generation of steam, when the hydrogen content of the initial fuel gas is not less than 30%; the pressure of the newly injected oxygen in the cathode tail gas storage tank is not higher than 4MPa; the cathode tail gas After being pressurized by the compressor, the pressure is not higher than 2MPa; the first preset temperature of the fuel gas entering the fuel cell anode after preheating is not lower than 700°C; after the first medium-pressure steam is produced from the anode tail gas, its temperature Not lower than 400°C. After the first low-pressure steam is produced, its temperature is not lower than 200°C. The second preset temperature of the oxygen entering the fuel cell cathode after preheating is not lower than 700°C; after the cathode tail gas produces the second medium-pressure steam, the temperature is not lower than 400°C; after the second low-pressure steam is produced, the temperature is not lower than 700°C. below 150℃. In the entire power generation process, the total revenue generated by the cogeneration steam system's power generation and the total tonnage of medium-pressure steam and low-pressure steam produced is higher than the total revenue when fuel gas, oxygen and other related parameters are not within the preset range. Therefore, setting the relevant parameters of the process flow according to the range of fuel gas and oxygen related parameter setting requirements can better improve the efficiency of cogeneration and obtain better revenue effects.
本发明实施例的发电过程中联产蒸汽的系统,将燃料电池燃烧发电与蒸汽生产相结合,相比较于传统通过燃烧方式进行蒸汽生产的方式,减少了蒸汽生产过程中二氧化碳的排放,同时利用燃料电池的阳极尾气与阴极尾气进行蒸汽的产出,提高了阳极尾气与阴极尾气的余热品质,带来更好的经济效益。The co-generation steam system in the power generation process of the embodiment of the present invention combines fuel cell combustion power generation with steam production. Compared with the traditional method of steam production through combustion, it reduces carbon dioxide emissions during the steam production process and simultaneously utilizes The anode exhaust gas and cathode exhaust gas of the fuel cell produce steam, which improves the waste heat quality of the anode exhaust gas and cathode exhaust gas and brings better economic benefits.
应该明白,公开的过程中的步骤的特定顺序或层次是示例性方法的实例。基于设计偏好,应该理解,过程中的步骤的特定顺序或层次可以在不脱离本公开的保护范围的情况下得到重新安排。所附的方法权利要求以示例性的顺序给出了各种步骤的要素,并且不是要限于所述的特定顺序或层次。It is understood that the specific order or hierarchy of steps in the disclosed processes is an example of an exemplary approach. Based on design preferences, it is understood that the specific order or hierarchy of steps in the process may be rearranged without departing from the scope of the present disclosure. The accompanying method claims present elements of the various steps in a sample order, and are not intended to be limited to the specific order or hierarchy described.
在上述的详细描述中,各种特征一起组合在单个的实施方案中,以简化本公开。不应该将这种公开方法解释为反映了这样的意图,即,所要求保护的主题的实施方案需要清楚地在每个权利要求中所陈述的特征更多的特征。相反,如所附的权利要求书所反映的那样,本发明处于比所公开的单个实施方案的全部特征少的状态。因此,所附的权利要求书特此清楚地被并入详细描述中,其中每项权利要求独自作为本发明单独的优选实施方案。In the foregoing detailed description, various features are grouped together in single embodiments to simplify the disclosure. This method of disclosure is not to be interpreted as reflecting an intention that embodiments of the claimed subject matter require more features than are expressly recited in each claim. Rather, as the following claims reflect, this invention lies in less than all features of a single disclosed embodiment. Thus, the following claims are hereby expressly incorporated into the Detailed Description, with each claim standing on its own as a separate preferred embodiment of this invention.
上文的描述包括一个或多个实施例的举例。当然,为了描述上述实施例而描述部件或方法的所有可能的结合是不可能的,但是本领域普通技术人员应该认识到,各个实施例可以做进一步的组合和排列。因此,本文中描述的实施例旨在涵盖落入所附权利要求书的保护范围内的所有这样的改变、修改和变型。此外,就说明书或权利要求书中使用的术语“包含”,该词的涵盖方式类似于术语“包括”,就如同“包括”在权利要求中用 作衔接词所解释的那样。此外,使用在权利要求书的说明书中的任何一个术语“或者”是要表示“非排它性的或者”。The above description includes examples of one or more embodiments. Of course, it is impossible to describe all possible combinations of components or methods for describing the above embodiments, but those of ordinary skill in the art will recognize that the various embodiments can be further combined and arranged. Accordingly, the embodiments described herein are intended to embrace all such alterations, modifications and variations that fall within the scope of the appended claims. Furthermore, to the extent that the term "comprises" is used in the description or claims, the word is encompassed in a manner similar to the term "comprises" as if "comprises" were to be interpreted as a linking word in the claims. Furthermore, any term "or" used in the description of the claims is intended to mean "a non-exclusive or".

Claims (15)

  1. 一种发电过程中联产蒸汽的系统,其中,包括:燃料电池、供气单元、供氧单元、以及第一蒸汽生成单元和/或第二蒸汽生成单元;A system for co-generating steam during power generation, which includes: a fuel cell, a gas supply unit, an oxygen supply unit, and a first steam generation unit and/or a second steam generation unit;
    所述供气单元,与所述燃料电池的阳极相连,以为所述燃料电池提供燃料气;The gas supply unit is connected to the anode of the fuel cell to provide fuel gas for the fuel cell;
    所述供氧单元,与所述燃料电池的阴极相连,以为所述燃料电池提供氧气;The oxygen supply unit is connected to the cathode of the fuel cell to provide oxygen to the fuel cell;
    所述燃料电池,用于使用所述燃料气和所述氧气发电并产生阳极尾气和阴极尾气;The fuel cell is used to generate electricity using the fuel gas and the oxygen and produce anode exhaust gas and cathode exhaust gas;
    第一蒸汽生成单元,与所述阳极相连,用于利用所述阳极产生的阳极尾气与水进行换热产出蒸汽;A first steam generation unit, connected to the anode, is used to generate steam by exchanging heat with water between the anode exhaust gas generated by the anode;
    第二蒸汽生成单元,与所述阴极相连,用于利用所述阴极产生的阴极尾气与水进行换热产出蒸汽。The second steam generation unit is connected to the cathode and is used to generate steam by exchanging heat with water between the cathode exhaust gas generated by the cathode.
  2. 如权利要求1所述的系统,其中,所述供气单元包括:净化器和供气预热装置;The system according to claim 1, wherein the air supply unit includes: a purifier and an air supply preheating device;
    所述净化器用于对初始燃料气的杂质处理;The purifier is used to treat impurities in the initial fuel gas;
    所述供气预热装置包括第一换热器与第二换热器,所述第一换热器与所述净化器连接,所述第二换热器与所述燃料电池连接;所述供气预热装置用于对处理后的燃料气进行预热处理,使所述燃料气达到第一预设温度后提供到燃料电池的阳极。The air supply preheating device includes a first heat exchanger and a second heat exchanger, the first heat exchanger is connected to the purifier, and the second heat exchanger is connected to the fuel cell; The gas supply preheating device is used to preheat the treated fuel gas so that the fuel gas reaches the first preset temperature and is supplied to the anode of the fuel cell.
  3. 如权利要求1所述的系统,其中,所述供氧单元,包括:阴极尾气储罐、压缩机及供氧预热装置;The system according to claim 1, wherein the oxygen supply unit includes: a cathode exhaust gas storage tank, a compressor and an oxygen supply preheating device;
    所述阴极尾气储罐,与所述第二蒸汽生成单元相连,用于储存阴极尾气和/或新注入的氧气,并将阴极尾气与新注入的氧气混合得到混合氧气,所述阴极尾气为未反应的氧气;The cathode tail gas storage tank is connected to the second steam generation unit and is used to store the cathode tail gas and/or newly injected oxygen, and mix the cathode tail gas and the newly injected oxygen to obtain mixed oxygen, and the cathode tail gas is not yet reacting oxygen;
    所述压缩机,与所述阴极尾气储罐相连,用于压缩阴极尾气、新注入的氧气或混合氧气使其达到预设压力;The compressor is connected to the cathode tail gas storage tank and is used to compress the cathode tail gas, newly injected oxygen or mixed oxygen to reach a preset pressure;
    所述供氧预热装置用于对压缩后的阴极尾气、新注入的氧气或混合氧气进行预热使其达到第二预设温度。The oxygen supply preheating device is used to preheat the compressed cathode tail gas, newly injected oxygen or mixed oxygen to reach the second preset temperature.
  4. 如权利要求1所述的系统,其中,The system of claim 1, wherein,
    所述第一蒸汽生成单元包括第三换热器和第四换热器,所述第三换热器与所述燃料电池阳极相连以利用阳极尾气与水进行换热产出第一中压蒸汽,所述第四换热器与所述第三换热器相连以利用阳极尾气与水进行换热产出第一低压蒸汽;The first steam generation unit includes a third heat exchanger and a fourth heat exchanger. The third heat exchanger is connected to the anode of the fuel cell to use the anode exhaust gas and water to exchange heat to produce the first medium pressure steam. , the fourth heat exchanger is connected to the third heat exchanger to use the anode exhaust gas and water to exchange heat to produce the first low-pressure steam;
    所述第二蒸汽生成单元包括第五换热器与第六换热器,所述第五换热器与所述燃料电池阴极相连以利用阴极尾气产出第二中压蒸汽,所述第六换热器与所述第五换热器相 连以利用阴极尾气产出第二低压蒸汽。The second steam generation unit includes a fifth heat exchanger and a sixth heat exchanger. The fifth heat exchanger is connected to the cathode of the fuel cell to generate second medium-pressure steam using cathode exhaust gas. The sixth heat exchanger The heat exchanger is connected to the fifth heat exchanger to produce second low-pressure steam using the cathode exhaust gas.
  5. 如权利要求4所述的系统,其中,还包括第三蒸汽生成单元,The system of claim 4, further comprising a third steam generation unit,
    所述第三蒸汽生成单元包括阳气尾气燃烧器、第七换热器、第八换热器及第九换热器;The third steam generation unit includes a positive gas tail gas burner, a seventh heat exchanger, an eighth heat exchanger and a ninth heat exchanger;
    所述阳气尾气燃烧器与所述第四换热器相连用于燃烧阳极尾气中未反应的燃料气以产生燃烧产物,且所述阳气尾气燃烧器与供氧预热装置及第二换热器相连以使所述燃烧产物为所述燃料气及氧气预热;The positive gas tail gas burner is connected to the fourth heat exchanger for burning unreacted fuel gas in the anode tail gas to produce combustion products, and the positive gas tail gas burner is connected to an oxygen supply preheating device and a second heat exchanger. The heater is connected to allow the combustion products to preheat the fuel gas and oxygen;
    所述第七换热器与所述第二换热器及供氧预热装置相连以利用用于预热后的所述燃烧产物与水换热生产第三中压蒸汽;The seventh heat exchanger is connected to the second heat exchanger and the oxygen supply preheating device to produce third medium-pressure steam by exchanging heat between the preheated combustion products and water;
    所述第八换热器与所述第七换热器相连以利用燃烧产物与水进行换热生产第三低压蒸汽;The eighth heat exchanger is connected to the seventh heat exchanger to utilize combustion products and water to exchange heat to produce third low-pressure steam;
    所述第九换热器与所述第八换热器相连以生产热水并放空燃烧产物。The ninth heat exchanger is connected to the eighth heat exchanger to produce hot water and vent combustion products.
  6. 如权利要求5所述的系统,其中,所述第八换热器与所述第一换热器相连,以利用第三低压蒸汽对所述燃料气进行预热。The system of claim 5, wherein the eighth heat exchanger is connected to the first heat exchanger to preheat the fuel gas using third low pressure steam.
  7. 一种发电过程中联产蒸汽的方法,其中,包括:利用如权利要求1-6任一项所述的发电过程中联产蒸汽的系统进行蒸汽的生产,其步骤如下:A method for co-generating steam in a power generation process, which includes: using the system for co-generating steam in a power generation process as claimed in any one of claims 1 to 6 to produce steam, the steps of which are as follows:
    供气单元为燃料电池的阳极提供燃料气,供氧单元为燃料电池的阴极提供氧气;The gas supply unit provides fuel gas for the anode of the fuel cell, and the oxygen supply unit provides oxygen for the cathode of the fuel cell;
    利用所述燃料气与氧气在燃料电池中进行发电反应并产生阳极尾气和阴极尾气;Utilize the fuel gas and oxygen to perform a power generation reaction in a fuel cell and generate anode exhaust gas and cathode exhaust gas;
    第一蒸汽生成单元利用所述阳极尾气与水进行换热产出蒸汽,和/或第二蒸汽生成单元利用所述阴极尾气与水进行换热产出蒸汽。The first steam generation unit uses the anode tail gas and water to exchange heat to produce steam, and/or the second steam generation unit uses the cathode tail gas and water to exchange heat to produce steam.
  8. 如权利要求7所述的方法,其中,所述供气单元为所述燃料电池的阳极提供燃料气,包括:The method of claim 7, wherein the gas supply unit provides fuel gas for the anode of the fuel cell, comprising:
    所述供气单元对初始燃料气进行净化处理并预热,使所述燃料气达到第一预设温度后提供给燃料电池的阳极进行反应。The gas supply unit purifies and preheats the initial fuel gas so that the fuel gas reaches a first preset temperature and is supplied to the anode of the fuel cell for reaction.
  9. 如权利要求8所述的方法,其中,所述供氧单元为所述燃料电池的阴极提供氧气,包括:The method of claim 8, wherein the oxygen supply unit provides oxygen to the cathode of the fuel cell, comprising:
    所述供氧单元将新注入的氧气、阴极尾气、或新注入的氧气和阴极尾气的混合氧气进行压缩和预热,使其达到预设压力和第二预设温度后,提供给所述燃料电池的阴极进行反应。The oxygen supply unit compresses and preheats the newly injected oxygen, the cathode tail gas, or the mixed oxygen of the newly injected oxygen and the cathode tail gas, so that it reaches the preset pressure and the second preset temperature, and then provides it to the fuel The reaction takes place at the cathode of the battery.
  10. 如权利要求7所述的方法,其中,所述第一蒸汽生成单元利用所述阳极尾气与 水进行换热产出蒸汽,和/或第二蒸汽生成单元利用所述阴极尾气与水进行换热产出蒸汽,包括:The method of claim 7, wherein the first steam generation unit utilizes the anode exhaust gas and water to exchange heat to produce steam, and/or the second steam generation unit utilizes the cathode exhaust gas and water to exchange heat Produces steam including:
    所述第一蒸汽生成单元利用所述阳极尾气在第三换热器及第四换热器内进行换热产出第一中压蒸汽和第一低压蒸汽;The first steam generation unit uses the anode tail gas to perform heat exchange in the third heat exchanger and the fourth heat exchanger to produce first medium pressure steam and first low pressure steam;
    所述第二蒸汽生成单元利用所述阴极尾气在第五换热器及第六换热器内进行换热产出第二中压蒸汽和第二低压蒸汽。The second steam generation unit uses the cathode exhaust gas to perform heat exchange in the fifth heat exchanger and the sixth heat exchanger to produce second medium pressure steam and second low pressure steam.
  11. 如权利要求7所述的方法,其中,还包括:The method of claim 7, further comprising:
    所述第三蒸汽生成单元利用未反应的燃料气燃烧后的燃烧产物在第七换热器、第八换热器及第九换热器内进行换热产出第三中压蒸汽、第三低压蒸汽和热水。The third steam generation unit uses the combustion products of the unreacted fuel gas to perform heat exchange in the seventh heat exchanger, the eighth heat exchanger and the ninth heat exchanger to produce third medium pressure steam, third Low pressure steam and hot water.
  12. 如权利要求11所述的方法,其中,The method of claim 11, wherein,
    所述第三低压蒸汽为所述燃料气进行预热;The third low-pressure steam preheats the fuel gas;
    所述未反应的燃料气燃烧后的燃烧产物为所述燃料气及所述氧气进行预热。The combustion products of the unreacted fuel gas are preheated for the fuel gas and the oxygen.
  13. 如权利要求9所述的方法,其中,所述初始燃料气氢气含量不低于30%;The method of claim 9, wherein the hydrogen content of the initial fuel gas is not less than 30%;
    所述阴极尾气储罐中新注入的氧气的压力不高于4MPa;The pressure of newly injected oxygen in the cathode tail gas storage tank is not higher than 4MPa;
    所述阴极尾气经压缩机增压后,压力不高于2MPa。After the cathode exhaust gas is pressurized by the compressor, the pressure is not higher than 2MPa.
  14. 如权利要求8所述的方法,其中,所述燃料气经过预热进入所述燃料电池阳极的第一预设温度不低于700℃;所述阳极尾气生产第一中压蒸汽后,其温度不低于400℃,生产第一低压蒸汽后,其温度不低于200℃。The method of claim 8, wherein the first preset temperature of the fuel gas entering the fuel cell anode after preheating is not lower than 700°C; after the anode exhaust gas produces the first medium-pressure steam, its temperature Not lower than 400°C. After the first low-pressure steam is produced, its temperature is not lower than 200°C.
  15. 如权利要求9所述的方法,其中,The method of claim 9, wherein,
    所述氧气经过预热进入所述燃料电池阴极的第二预设温度不低于700℃;阴极尾气生产第二中压蒸汽后,温度不低于400℃,生产第二低压蒸汽后,温度不低于150℃。The second preset temperature of the oxygen entering the fuel cell cathode after preheating is not lower than 700°C; after the cathode tail gas produces the second medium-pressure steam, the temperature is not lower than 400°C; after the second low-pressure steam is produced, the temperature is not lower than 700°C. Below 150℃.
PCT/CN2022/138873 2022-08-05 2022-12-14 Method and system for co-producing steam in power generation process WO2024027073A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202210939171.5A CN117553286A (en) 2022-08-05 2022-08-05 Method and system for co-producing steam in power generation process
CN202210939171.5 2022-08-05

Publications (1)

Publication Number Publication Date
WO2024027073A1 true WO2024027073A1 (en) 2024-02-08

Family

ID=89822049

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2022/138873 WO2024027073A1 (en) 2022-08-05 2022-12-14 Method and system for co-producing steam in power generation process

Country Status (2)

Country Link
CN (1) CN117553286A (en)
WO (1) WO2024027073A1 (en)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20130115894A (en) * 2012-04-13 2013-10-22 한국기계연구원 Anode off gas recirculation fuel cell system using ejector
CN104409750A (en) * 2014-10-28 2015-03-11 航天新长征电动汽车技术有限公司 Fuel-cell tail gas circulation system
DE102016012420A1 (en) * 2016-10-18 2018-04-19 Linde Aktiengesellschaft Method and system for preheating a fuel of a burner
CN112864432A (en) * 2019-11-27 2021-05-28 国家能源投资集团有限责任公司 System and method for generating power by using synthesis gas high-temperature fuel cell
CN114586207A (en) * 2019-12-25 2022-06-03 富士电机株式会社 Fuel cell system and operation method

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20130115894A (en) * 2012-04-13 2013-10-22 한국기계연구원 Anode off gas recirculation fuel cell system using ejector
CN104409750A (en) * 2014-10-28 2015-03-11 航天新长征电动汽车技术有限公司 Fuel-cell tail gas circulation system
DE102016012420A1 (en) * 2016-10-18 2018-04-19 Linde Aktiengesellschaft Method and system for preheating a fuel of a burner
CN112864432A (en) * 2019-11-27 2021-05-28 国家能源投资集团有限责任公司 System and method for generating power by using synthesis gas high-temperature fuel cell
CN114586207A (en) * 2019-12-25 2022-06-03 富士电机株式会社 Fuel cell system and operation method

Also Published As

Publication number Publication date
CN117553286A (en) 2024-02-13

Similar Documents

Publication Publication Date Title
CN110544785B (en) Natural gas autothermal reforming proton exchange membrane fuel cell distributed cogeneration system and method
CN111525166B (en) Hybrid high temperature fuel cell power generation system and method
WO2010044113A1 (en) Apparatus and method for capturing carbon dioxide from combustion exhaust gas and generating electric energy by means of mcfc systems
CN109686998A (en) Association circulating power generation system based on the cooling fuel cell of gas turbine
CN108400358A (en) Solid oxide fuel cell oven gas electrification technique and device
CN114420972A (en) PEMFC power generation system using ammonia decomposition gas as raw material
CN101540410B (en) Natural gas hydrogen production and proton-exchange film fuel cell integrated generation method and device thereof
CN115395047A (en) Methane-electricity-hydrogen reversible solid oxide fuel cell system with shared system components
WO2024213050A1 (en) Green methanol preparation process and system
CN212011147U (en) Hybrid high-temperature fuel cell power generation system
CN209266502U (en) Association circulating power generation system based on the cooling fuel cell of gas turbine
CN117512629A (en) Natural gas vapor self-heating conversion and water electrolysis mixed power hydrogen production and fuel cell coupled cogeneration system
CN218710890U (en) Gas power generation coupling SOEC hydrogen production system
CN116759614A (en) Ammonia-methane dual-fuel power generation system and method
WO2024027073A1 (en) Method and system for co-producing steam in power generation process
CN114893264B (en) Combining green hydrogen with CO 2 Coal-fired oxygen-enriched combustion power generation system and method for resource utilization
CN1379494A (en) Electric generation system combining solid oxide fuel battery with turbogenerator
CN201402833Y (en) Battery integration generating device based on natural-gas-prepared hydrogen and proton exchange membrane fuel
CN211789285U (en) Purge gas utilization system based on fuel cell combined power generation
CN114522518A (en) Carbon-containing recycling gas power plant low-cost carbon emission reduction system and method
CN113921863A (en) Power generation system and method for molten carbonate fuel cell
CN218934568U (en) Gas power generation coupling SOEC zero carbon emission system
CN115939470B (en) Anode tail gas double-reflux solid oxide fuel cell system and operation method thereof
CN1240156C (en) Coal gasification two stage high temperature fuel battery electric generating system
CN210723233U (en) Cogeneration device of solid oxide fuel cell and process heating furnace

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 22953861

Country of ref document: EP

Kind code of ref document: A1