CN109326805B - Solid oxide fuel cell power generation system and process - Google Patents
Solid oxide fuel cell power generation system and process Download PDFInfo
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- CN109326805B CN109326805B CN201811024426.5A CN201811024426A CN109326805B CN 109326805 B CN109326805 B CN 109326805B CN 201811024426 A CN201811024426 A CN 201811024426A CN 109326805 B CN109326805 B CN 109326805B
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- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
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- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
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- H01M2008/1293—Fuel cells with solid oxide electrolytes
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Abstract
The invention provides a solid oxide fuel cell power generation system and a process, which comprises a solid oxide fuel cell, a fuel supply system, an air supply system and a waste heat recovery system, wherein a heat exchanger and a steam generator are utilized to recover heat energy in tail gas of the solid oxide fuel cell, the usage amount of circulating cooling water is reduced, the process cost is reduced, and the byproduct saturated steam is increased, so that the amount of the produced saturated steam is increased, the consumption amount of circulating water is reduced, and the comprehensive efficiency is improved.
Description
Technical Field
The invention belongs to the field of solid oxide fuel cells, and particularly relates to a solid oxide fuel cell power generation system and a solid oxide fuel cell power generation process.
Background
A solid oxide fuel cell is a power generation device that converts chemical energy into electrical energy, and in a known solid oxide fuel cell system, for a waste heat recovery system, at the cathode: after the gas from the cathode preheats the air at the inlet of the cathode, one part of the gas is used for catalytic combustion, and the other part of the gas needs to be cooled by circulating water and then is discharged.
At the cathode, the cooled cathode tail gas needs to be discharged, so that zero emission cannot be achieved; from the energy-saving perspective, for the cathode inlet, after the cathode waste gas preheats a large amount of cathode inlet gas, the temperature is very low, high-level heat cannot be generated and reused, and the cathode waste gas can only be cooled by using circulating water and then discharged, so that the heat cannot be reasonably utilized, and a large amount of circulating water is consumed, which is a resource waste and is not beneficial to energy conservation.
Disclosure of Invention
Aiming at the problem of waste of heat energy of cathode tail gas of the solid oxide fuel cell in the prior art, the invention provides the tail gas treatment system of the solid oxide fuel cell, which realizes full utilization of heat energy of the cathode tail gas of the solid oxide fuel cell and meets the requirement of zero emission.
The invention discloses a solid oxide fuel cell power generation system which comprises a solid oxide fuel cell, a fuel supply system, an air supply system and a waste heat recovery system.
The fuel supply system comprises a first heat exchanger, a second heat exchanger and a pre-reformer, wherein a fuel input pipeline is connected with an inlet of a fuel channel of the first heat exchanger, an outlet of the fuel channel of the first heat exchanger is connected with a fuel inlet of the pre-reformer after passing through the fuel channel of the second heat exchanger, and an outlet of the pre-reformer is connected with an anode inlet of the solid oxide fuel cell after passing through a fuel channel of the third heat exchanger.
The air supply system comprises an air input pipeline connected with a cathode inlet of the solid oxide fuel cell and a fourth heat exchanger arranged on the air input pipeline.
The waste heat recovery system comprises a catalytic oxidation burner, a first steam generator, a second steam generator, a fifth heat exchanger, a sixth heat exchanger, a circulating compressor and a gas-liquid separator, wherein a cathode tail gas output pipeline of the solid oxide fuel cell passes through the fourth heat exchanger and then is connected with a cathode tail gas inlet of the second steam generator, a cathode tail gas output pipeline of the second steam generator passes through the circulating compressor and then is converged with an air input pipeline of an air supply system, an anode tail gas output pipeline of the solid oxide fuel cell sequentially passes through a tail gas channel of the third heat exchanger, the second heat exchanger and the first heat exchanger and then is converged with one path of air input pipeline and then is connected with an inlet of the catalytic oxidation burner, a gas outlet of the catalytic oxidation burner is connected with an anode tail gas inlet of the pre-reformer through a pipeline, and an anode tail gas output pipeline of the pre-reformer enters the first steam generator through a gas inlet, the first steam generator is connected with a first branch pipe, the first branch pipe is connected with a heat exchange channel of the fifth heat exchanger and a heat exchange channel of the sixth heat exchanger, the first branch pipe is connected with an inlet of the gas-liquid separator, a gas outlet pipeline of the gas-liquid separator and another branch pipe of the first steam generator are converged into a total tail gas output pipeline or independently used as a tail gas output pipeline, a liquid output pipeline of the gas-liquid separator is divided into two branch pipes after passing through another heat exchange channel of the fifth heat exchanger, one branch pipe is connected with a pipeline between the first heat exchanger and the second heat exchanger after passing through the first steam generator, the other branch pipe is connected with a liquid inlet of the second steam generator, and a steam output pipeline of the second steam generator is.
Preferably, a centrifugal pump for providing power for liquid is arranged on a liquid output pipeline of the gas-liquid separator.
Preferably, the circulation compressor is a labyrinth compressor.
Preferably, the other heat exchange channel of the sixth heat exchanger is connected with a cold water pipe, and an outlet of the heat exchange channel is connected with a hot water output pipeline.
Preferably, the system also comprises a control system for controlling the operation of the whole power generation system and a power output system for outputting power to the downstream.
The invention also provides a solid oxide fuel cell power generation process, which comprises the following steps:
(1) the fuel is heated to 200-450 ℃, preferably about 300-400 ℃ through heat exchange with anode tail gas from the anode of the solid oxide fuel cell in the first heat exchanger and the second heat exchanger, then enters the pre-reformer for reaction, the pre-reformed gas is heated to 600-750 ℃, preferably 650-720 ℃ through heat exchange with the anode tail gas directly coming out of the anode of the solid oxide fuel cell in the third heat exchanger, then enters the anode of the solid oxide fuel cell, the air is heated to 600-750 ℃ through heat exchange with cathode tail gas from the cathode of the solid oxide fuel cell through an air input pipeline and a fourth heat exchanger, preferably 650-720 ℃, then enters the cathode of the solid oxide fuel cell, and the fuel and the oxygen in the air undergo oxidation-reduction reaction in the solid oxide fuel cell to generate electric energy, wherein the anode tail gas from the solid oxide fuel cell sequentially enters the third heat exchanger and the third heat exchanger, The second heat exchanger and the first heat exchanger are used for supplying heat, the heat is mixed with air after being discharged from the first heat exchanger and enters the catalytic oxidation burner for burning, and the tail gas (the high-temperature gas with the temperature of about 800-;
(2) the cathode tail gas (temperature is generally 700-900 ℃, preferably 750-850 ℃) generated by the solid oxide fuel cell enters a fourth heat exchanger through a cathode tail gas output pipeline to exchange heat with air (the cathode tail gas is heated to about 600-750 ℃), then enters a second steam generator, low-temperature liquid is heated in the second steam generator to generate saturated steam (the self temperature is reduced to 150-400 ℃, usually 200-300 ℃), the cooled cathode tail gas enters a circulating compressor to be pressurized (for example, to 150-400KPa, further 200-300KPa) and then is merged with air, enters the fourth heat exchanger to exchange heat with the cathode tail gas generated by the solid oxide fuel cell to raise the temperature to 600-750 ℃, preferably 650-720 ℃ and then enters the cathode of the solid oxide fuel cell together.
The tail gas (the temperature is usually reduced to 300-, the water obtained by separation in the gas-liquid separator is discharged from a liquid output pipeline, is pressurized by a pump and then enters a fifth heat exchanger (exchanges heat with gas out of the first steam generator) to be heated and then is divided into two branches, the first branch enters the first steam generator, the generated saturated steam is converged with fuel between the first heat exchanger and the second heat exchanger, the second branch enters the second steam generator (the liquid volume ratio of the first branch to the second branch can be, for example, 1:0.2-10 according to requirements), the cathode tail gas out of the fourth heat exchanger is heated and heated to become saturated steam, and the saturated steam is sent out by a saturated steam output pipeline (for example, as external steam supply). Wherein the sixth heat exchanger introduces circulating water (e.g., 20-40 ℃, further about 32 ℃) to exchange heat with the gas, and the temperature of the gas entering the sixth heat exchanger is reduced to preferably below 45 ℃, e.g., 30-45 ℃, further about 40 ℃.
Generally, the temperature of anode tail gas generated by the solid oxide fuel cell is 700-.
Wherein the fuel in the step (1) is pipeline gas, and the component of the pipeline gas is CO21-2V％、CH490-95V％、N21-3V％、C2H63-5V％、C3H80.8-2V％、C3H60.2-0.5V％。
Wherein the composition of the mixed gas in the step (1) is H2、CO、CO2And H2O, the water-carbon ratio is 1-5: 1, preferably 2 to 4: 1.
wherein, after the cathode tail gas is pressurized by the circulating compressor in the step (2), the pressure is increased to 150-400KPa, preferably 180-300 KPa.
Wherein, the temperature of the saturated steam generated in the first steam generator and the second steam generator in the step (2) is 120-.
The invention has the beneficial effects that: the invention utilizes the heat exchanger and the steam generator to recover the heat energy in the tail gas of the solid oxide fuel cell, realizes the secondary utilization of the heat energy in the tail gas, mixes the cooled cathode tail gas with air and reenters the solid oxide fuel cell, simultaneously reduces the using amount of circulating water, simplifies the process, reduces the process cost, saves the cooling procedure of the cathode circulating water, and increases the byproduct saturated steam, thereby improving the amount of the produced saturated steam, reducing the consumption of the circulating water and improving the comprehensive efficiency.
Drawings
Fig. 1 is a schematic process flow diagram of a prior art solid oxide fuel cell power generation system.
Fig. 2 is a schematic process flow diagram of a solid oxide fuel cell power generation system of the present invention.
Description of reference numerals:
e101, E102, E103, E105, E107, E108, E109: a heat exchanger;
e106: first steam generator, E104: a second steam generator;
f101: catalytic oxidation burner, R101: prereformer, V101: gas-liquid separator, C101: compressor, P101: pump, SOFC: a solid oxide fuel cell.
Detailed Description
The invention is further illustrated by the following figures and examples.
As shown in fig. 2, the present invention provides a solid oxide fuel cell power generation system, which comprises a solid oxide fuel cell, a fuel supply system, an air supply system, and a waste heat recovery system,
the fuel supply system comprises a first heat exchanger E101, a second heat exchanger E102 and a pre-reformer R101, wherein a fuel input pipeline is connected with the inlet of a fuel channel of the first heat exchanger E101, the outlet of the fuel channel of the first heat exchanger E101 is connected with the fuel inlet of the pre-reformer R101 after passing through the fuel channel of the second heat exchanger E102, the fuel outlet of the pre-reformer R101 is connected with the anode inlet of the solid oxide fuel cell after passing through the fuel channel of the third heat exchanger E103 through a pipeline,
the air supply system comprises an air input pipeline connected with the cathode inlet of the solid oxide fuel cell and a fourth heat exchanger E105 arranged on the air input pipeline,
the waste heat recovery system comprises a catalytic oxidation combustor F101, a first steam generator E106, a second steam generator E104, a fifth heat exchanger E107, a sixth heat exchanger E108, a circulating compressor C101 and a gas-liquid separator V101, a cathode tail gas output pipeline of the solid oxide fuel cell passes through the fourth heat exchanger E105 and then is connected to a cathode tail gas inlet of the second steam generator E104, a cathode tail gas output pipeline of the second steam generator E104 passes through the circulating compressor C101 and then is converged with an air input pipeline of an air supply system, an anode tail gas output pipeline of the solid oxide fuel cell sequentially passes through a tail gas channel of the third heat exchanger E103, the second heat exchanger E102 and the first heat exchanger E101 and then is converged with one air input pipeline to be connected with an inlet of the catalytic oxidation combustor F101, a gas outlet pipeline of the catalytic oxidation combustor F101 is connected to an anode tail gas inlet of the pre-reformer R101, an anode tail gas output pipeline of the pre-reformer R101 enters the first steam generator E106 through a gas inlet of the first steam generator E106, is divided into two branch pipes after being discharged from the first steam generator E106, one branch pipe is connected with a heat exchange channel of each of the fifth heat exchanger E107 and the sixth heat exchanger E108 in sequence, then the gas outlet pipeline of the gas-liquid separator V101 and the other branch of the first steam generator E106 are converged into a total tail gas output pipeline or are independently used as a tail gas output pipeline, the liquid output pipeline of the gas-liquid separator V101 is divided into two branch pipes after passing through the other heat exchange channel of the fifth heat exchanger E107, one branch pipe is connected to the pipeline between the first heat exchanger and the second heat exchanger after passing through the first steam generator E106, the other branch pipe is connected to the liquid inlet of the second steam generator E104, and the steam output pipeline of the second steam generator E104 is an external steam supply pipeline.
The liquid output pipeline of the gas-liquid separator V101 is preferably provided with a centrifugal pump P101 for providing power for liquid.
The recycle compressor is preferably a labyrinth compressor.
And the other heat exchange channel of the sixth heat exchanger is connected with a cold water pipe, and the outlet of the heat exchange channel is connected with a hot water output pipeline.
The system also includes a control system for controlling the operation of the overall power generation system and a power output system for outputting power to a downstream location.
The invention also provides a solid oxide fuel cell power generation process, which comprises the following steps:
(1) the fuel is heated to 200-450 ℃, preferably about 300-400 ℃ through heat exchange with anode tail gas from the anode of the solid oxide fuel cell in the first heat exchanger and the second heat exchanger, then enters the pre-reformer for reaction, the pre-reformed gas is heated to 600-750 ℃, preferably 650-720 ℃ through heat exchange with the anode tail gas directly coming out of the anode of the solid oxide fuel cell in the third heat exchanger, then enters the anode of the solid oxide fuel cell, the air is heated to 600-750 ℃ through heat exchange with cathode tail gas from the cathode of the solid oxide fuel cell through an air input pipeline and a fourth heat exchanger, preferably 650-720 ℃, then enters the cathode of the solid oxide fuel cell, and the fuel and the oxygen in the air undergo oxidation-reduction reaction in the solid oxide fuel cell to generate electric energy, wherein the anode tail gas from the solid oxide fuel cell sequentially enters the third heat exchanger and the third heat exchanger, The second heat exchanger and the first heat exchanger are used for supplying heat, the heat is mixed with air after being discharged from the first heat exchanger and enters the catalytic oxidation burner for burning, and the tail gas (the high-temperature gas with the temperature of about 800-;
(2) the cathode tail gas (temperature is generally 700-900 ℃, preferably 750-850 ℃) generated by the solid oxide fuel cell enters a fourth heat exchanger through a cathode tail gas output pipeline to exchange heat with air (the cathode tail gas is heated to about 600-750 ℃), then enters a second steam generator, low-temperature liquid is heated in the second steam generator to generate saturated steam (the self temperature is reduced to 150-400 ℃, usually 200-300 ℃), the cooled cathode tail gas enters a circulating compressor to be pressurized (for example, to 150-400KPa, further 200-300KPa) and then is merged with air, enters the fourth heat exchanger to exchange heat with the cathode tail gas generated by the solid oxide fuel cell to raise the temperature to 600-750 ℃, preferably 650-720 ℃ and then enters the cathode of the solid oxide fuel cell together.
The tail gas (the temperature is usually reduced to 300-, the first branch enters a first steam generator, the generated saturated steam is converged with fuel between the first heat exchanger and the second heat exchanger, the second branch enters a second steam generator, the saturated steam is heated and heated by cathode tail gas out of the fourth heat exchanger to become saturated steam, and the saturated steam is sent out by a saturated steam output pipeline (for example, as external steam supply). Wherein the sixth heat exchanger introduces circulating water (e.g., 20-40 ℃, further about 32 ℃) to exchange heat with the gas, and the temperature of the gas entering the sixth heat exchanger is reduced to preferably below 45 ℃, e.g., 30-45 ℃, further about 40 ℃.
Generally, the temperature of anode tail gas generated by the solid oxide fuel cell is 700-.
Wherein the fuel in the step (1) is pipeline gas, and the component of the pipeline gas is CO21-2V％、CH490-95V％、N21-3V％、C2H63-5V％、C3H80.8-2V％、C3H60.2-0.5V％。
Wherein the composition of the mixed gas in the step (1) is H2、CO、CO2And H2O, the water-carbon ratio is 1-5: 1, preferably 2 to 4: 1.
wherein, after the cathode tail gas is pressurized by the circulating compressor in the step (2), the pressure is increased to 150-400KPa, preferably 180-300 KPa.
Wherein, the temperature of the saturated steam generated in the first steam generator and the second steam generator in the step (2) is 120-.
Example 1
As shown in FIG. 2, in a solid oxide fuel cell system with 25kW, the operating temperature of the electric pile is 750 ℃, the power generation efficiency is 60%, and the operating pressure of the system is 200 kPa.
(1) The fuel passes through a gas pipeline (the composition is CO)21.52V％、CH490.11V％、N22.09V％、C2H64.70V％、C3H81.09V％、C3H60.49V%, gas transmission amount of 3.26kg/H, pressure of 200KPa) is heated by a first heat exchanger E101 and a second heat exchanger E102 and then enters a prereformer R101, the prereformer R101 outputs mixed gas with the temperature of 350 ℃, and the mixed gas composition is H2、CO、CO2And H2The water-carbon ratio is 3.37:1, the mixed gas is subjected to heat exchange through a third heat exchanger E103 to be heated to 700 ℃, then enters the anode of the solid oxide fuel cell SOFC, air passes through an air input pipeline (the flow rate of oxygen in the air is 10.24kg/h, the pressure is 200kPa), is subjected to heat exchange through a fourth heat exchanger E105 to be heated to 700 ℃, then enters the cathode of the solid oxide fuel cell SOFC, and the fuel and the oxygen in the air are subjected to oxidation-reduction reaction in the solid oxide fuel cell to generate electric energy;
(2) the temperature of cathode tail gas generated by the solid oxide fuel cell SOFC is 800 ℃, the flow rate is 686.49kg/h, the cathode tail gas enters a fourth heat exchanger E105 through a cathode tail gas output pipeline, air is preheated to about 700 ℃, then the cathode tail gas enters a second steam generator, low-temperature liquid is heated in the second steam generator to generate saturated steam (the steam yield is 31.01kg/h, the saturated steam temperature is 120 ℃, the pressure is 188.94KPa), the temperature of the cathode tail gas is reduced to 250 ℃, the cooled cathode tail gas enters a circulating compressor to be pressurized to 195KPa and then is converged with the air, the cathode tail gas is heated to 700 ℃ through the fourth heat exchanger E105 and then enters the cathode of the solid oxide fuel cell together,
the anode tail gas generated by the solid oxide fuel cell enters a third heat exchanger E103 through an anode tail gas output pipeline, the prereformed gas is preheated to about 700 ℃, then the anode tail gas sequentially passes through a second heat exchanger E102 and a first heat exchanger E101 to preheat supplied fuel in a stepwise manner, then the fuel is mixed with a path of air (the gas transmission amount is 7.71kg/h) and then enters a catalytic oxidation burner F103 together, the anode tail gas is fully combusted, high-temperature gas with the temperature of about 850 ℃ is output from the catalytic oxidation burner, the high-temperature gas enters a prereformer R102 through a pipeline to heat the prereformer R102 to 350 ℃, the high-temperature gas enters a first steam generator E106, low-temperature liquid in the first steam generator is heated to generate saturated steam (the steam yield is 10.64kg/h, the saturated steam temperature is 150 ℃, the pressure is 468kpa), the gas discharged from the first steam generator is divided into two paths, and one path of gas is sequentially subjected to heat exchange with liquid water from a gas-liquid separator V101 and circulating water in fifth heat exchanger E107 and E And a liquid separator V101, wherein the gas separated in the gas-liquid separator is converged with the other path of gas from the first steam generator E106 through a gas output pipeline of the gas-liquid separator and then discharged out of the system, the hot water separated in the gas-liquid separator is pressurized through a pump P101 through a liquid output pipeline and then is heated through a fifth heat exchanger E107 and then is divided into two paths, one path of hot water enters the first steam generator E106, the generated saturated steam is converged with the fuel between the first heat exchanger and the second heat exchanger, the other path of hot water enters the second steam generator E104, and the cathode tail gas from the fourth heat exchanger E105 is heated and heated to become saturated steam which is sent out through a saturated steam output pipeline.
Comparative example 1
As shown in figure 1, the operating temperature of a pile of a solid oxide fuel cell system of 25kW is 750 ℃, the power generation efficiency is 60%, and the operating pressure of the system is 200 kPa.
(1) The fuel passes through a gas pipeline (the composition is CO)21.52V％、CH490.11V％、N22.09V％、C2H64.70V％、C3H81.09V％、C3H60.49V% gas transmissionThe amount is 3.26kg/H, the pressure is 200KPa), the mixture is heated by a heat exchanger and enters a prereformer, the prereformer outputs a mixed gas with the temperature of 350 ℃, and the mixed gas comprises H2、CO、CO2And H2The water-carbon ratio is 3.37:1, the mixed gas is heated to 700 ℃ through heat exchange of a third heat exchanger, then enters the anode of the solid oxide fuel cell, the air enters the cathode of the solid oxide fuel cell after being heated to 700 ℃ through heat exchange of a circulating compressor and the heat exchanger through an air input pipeline (the flow rate of oxygen in the air is 10.24kg/h, and the pressure is 200kPa), and the fuel and the oxygen in the air generate oxidation-reduction reaction in the solid oxide fuel cell to generate electric energy;
(2) the method comprises the steps that cathode tail gas output by a solid oxide fuel cell passes through a heat exchanger, then is mixed with cooled anode tail gas, and enters a catalytic combustor, the tail gas after catalytic combustion is heated to 350 ℃ by a pre-reformer, air provided by a cathode supply unit is preheated by the heat exchanger, then is sent to a steam generator to generate 10.63kg/h of saturated steam, is cooled to 40 ℃ by circulating water at 32 ℃ after being used for generating steam and preheating cooling water sent to the steam generator, and is discharged after leaving a system through a pipeline, wherein the required circulating water amount is 1346.07 kg/h. After the gas from the cathode of the solid oxide fuel cell is preheated to 700 ℃ by a heat exchanger and cooled to 79 ℃, a part of the gas enters a catalytic combustion chamber for combustion, and a part of the gas is cooled to 40 ℃ by 32 ℃ circulating water and then is discharged from the system through a pipeline, wherein the required amount of the circulating water is 730.83 kg/h.
In the prior art, for a 25kW SOFC system, the pipeline gas consumption is 3.26kg/h, the 150 ℃ (468kpa) saturated steam is produced by 10.63kg/h, the total consumption of circulating water is 2076.90kg/h, and the comprehensive efficiency of the system is 60.20%. In the system provided by the invention, the pipeline gas consumption is the same, only the oxygen supplement amount is increased by 10.24kg/h, and the saturated steam can be generated by 41.65kg/h, which is 3.92 times that in the prior art; the invention needs to consume 1345.92kg/h of circulating water, which is only 64.80 percent of the water consumption in the prior art; the total efficiency of the invention is 78.86%, which is improved by 18.66%. From the above data, it is apparent that: the invention greatly improves the comprehensive efficiency of the system, improves the amount of saturated steam, greatly reduces the consumption of circulating water, achieves the reasonable utilization of energy and realizes the purpose of energy conservation.
In the invention, the supplementary oxidant at the cathode side of the solid oxide fuel cell is oxygen from a factory compression system, and the gas from the cathode is recycled, thereby realizing 'zero emission' at the cathode side; the labyrinth compressor is used by the circulating compressor, so that the circulating temperature can reach 200-300 ℃ which is 100-200 ℃ higher than that of the common compressor, thereby reducing further processes of cooling and greatly raising the temperature of the circulating water, reducing the using amount of the circulating water, simplifying the process and reducing the process cost; because the generated energy is not changed, the generating efficiency is a fixed value, and the heat release of the galvanic pile is fixed under the ideal condition of not considering any loss, the cathode circulating water cooling process is saved, and the byproduct saturated steam is increased, thereby improving the amount of the produced saturated steam, reducing the consumption of the circulating water and improving the comprehensive efficiency.
Claims (15)
1. A solid oxide fuel cell power generation system, characterized by: the system comprises a solid oxide fuel cell, a fuel supply system, an air supply system and a waste heat recovery system;
the fuel supply system comprises a first heat exchanger, a second heat exchanger and a pre-reformer, wherein a fuel input pipeline is connected with an inlet of a fuel channel of the first heat exchanger, an outlet of the fuel channel of the first heat exchanger is connected with a fuel inlet of the pre-reformer after passing through the fuel channel of the second heat exchanger, and a fuel outlet of the pre-reformer is connected with an anode inlet of the solid oxide fuel cell after passing through the fuel channel of the third heat exchanger through a pipeline;
the air supply system comprises an air input pipeline connected with a cathode inlet of the solid oxide fuel cell and a fourth heat exchanger arranged on the air input pipeline;
the waste heat recovery system comprises a catalytic oxidation burner, a first steam generator, a second steam generator, a fifth heat exchanger, a sixth heat exchanger, a circulating compressor and a gas-liquid separator, wherein a cathode tail gas output pipeline of the solid oxide fuel cell passes through the fourth heat exchanger and then is connected with a cathode tail gas inlet of the second steam generator, a cathode tail gas output pipeline of the second steam generator passes through the circulating compressor and then is converged with an air input pipeline of an air supply system, an anode tail gas output pipeline of the solid oxide fuel cell sequentially passes through a tail gas channel of the third heat exchanger, the second heat exchanger and the first heat exchanger and then is converged with one air input pipeline to be commonly connected with an inlet of the catalytic oxidation burner, a gas outlet of the catalytic oxidation burner is connected with an anode tail gas inlet of the pre-reformer through a pipeline, and an anode tail gas output pipeline of the pre-reformer enters the first steam generator through a gas inlet of the, the first steam generator is connected with a first branch pipe, the first branch pipe is connected with a heat exchange channel of the fifth heat exchanger and a heat exchange channel of the sixth heat exchanger, the first branch pipe is connected with an inlet of the gas-liquid separator, a gas outlet pipeline of the gas-liquid separator and another branch pipe of the first steam generator are converged into a total tail gas output pipeline or independently used as a tail gas output pipeline, a liquid output pipeline of the gas-liquid separator is divided into two branch pipes after passing through another heat exchange channel of the fifth heat exchanger, one branch pipe is connected with a pipeline between the first heat exchanger and the second heat exchanger after passing through the first steam generator, the other branch pipe is connected with a liquid inlet of the second steam generator, and a steam output pipeline of the second steam generator is.
2. The power generation system of claim 1, wherein: and a centrifugal pump for providing power for liquid is arranged on a liquid output pipeline of the gas-liquid separator.
3. The power generation system of claim 1, wherein: the circulating compressor is a labyrinth compressor.
4. The power generation system of claim 1, wherein: wherein the sixth heat exchanger is provided with another heat exchange channel for circulating water to pass through.
5. A solid oxide fuel cell power generation process comprises the following steps:
(1) the fuel enters a pre-reformer for reaction after being heated to 450 ℃ through heat exchange with anode tail gas from the anode of the solid oxide fuel cell in a first heat exchanger and a second heat exchanger, the pre-reformed gas is heated to 600-750 ℃ through heat exchange with the anode tail gas directly coming out of the anode of the solid oxide fuel cell in a third heat exchanger and then enters the anode of the solid oxide fuel cell, air passes through an air input pipeline and a fourth heat exchanger through heat exchange with cathode tail gas from the cathode of the solid oxide fuel cell and then enters the cathode of the solid oxide fuel cell after being heated to 600-750 ℃, the fuel and oxygen in the air generate oxidation-reduction reaction in the solid oxide fuel cell to generate electric energy, wherein the anode tail gas from the solid oxide fuel cell sequentially enters the third heat exchanger, the second heat exchanger and the first heat exchanger for heat supply, mixing the tail gas with air after the tail gas is discharged from the first heat exchanger, feeding the mixture into a catalytic oxidation burner for burning, and heating the pre-reformer to 200-450 ℃;
(2) the cathode tail gas generated by the solid oxide fuel cell enters a fourth heat exchanger through a cathode tail gas output pipeline to exchange heat with air as described above, then enters a second steam generator, low-temperature liquid is heated in the second steam generator to generate saturated steam, the cooled cathode tail gas enters a circulating compressor to be pressurized to 150-plus-400 KPa and then is converged with air, enters the fourth heat exchanger to exchange heat with the cathode tail gas generated by the solid oxide fuel cell as described above, is heated to 600-plus-750 ℃, and then enters the cathode of the solid oxide fuel cell together;
the tail gas after catalytic combustion after the pre-reformer is heated enters a first steam generator, low-temperature liquid in the first steam generator is heated to generate saturated steam, gas discharged out of the first steam generator is divided into two paths, one path of gas enters a fifth heat exchanger and a sixth heat exchanger in sequence for heat exchange and then enters a gas-liquid separator, the gas separated from the gas-liquid separator is converged with the other path of gas discharged out of the first steam generator through a gas output pipeline of the gas-liquid separator and then is discharged out of a system or is discharged out of the system respectively, water separated from the gas-liquid separator is discharged from a liquid output pipeline, is pressurized by a pump, enters a fifth heat exchanger for heat exchange with the gas discharged out of the first steam generator and is divided into two branches after temperature rise, the first branch enters the first steam generator, the generated saturated steam is converged with fuel between the first heat exchanger and the second heat exchanger, and the second branch enters the second steam, and heating the cathode tail gas discharged from the fourth heat exchanger to raise the temperature of the cathode tail gas into saturated steam, and delivering the saturated steam to the outside through a saturated steam output pipeline, wherein circulating water is introduced into the sixth heat exchanger to exchange heat with gas.
6. The power generation process as claimed in claim 5, wherein in the step (1), the fuel is heated to 300-400 ℃ by heat exchange with the anode tail gas from the anode of the solid oxide fuel cell in the first and second heat exchangers and then enters the pre-reformer for reaction, the pre-reformed gas is heated to 650-720 ℃ by heat exchange with the anode tail gas directly coming out of the anode of the solid oxide fuel cell in the third heat exchanger and then enters the anode of the solid oxide fuel cell, the air is heated to 650-720 ℃ by heat exchange with the cathode tail gas from the cathode of the solid oxide fuel cell through the fourth heat exchanger by the air input pipeline and then enters the cathode of the solid oxide fuel cell, and the tail gas after catalytic combustion heats the pre-reformer to 300-400 ℃;
in the step (2), the cooled cathode tail gas enters a circulating compressor to be pressurized to 200-300KPa, and then is merged with air, enters a fourth heat exchanger to exchange heat with the cathode tail gas generated by the solid oxide fuel cell as described above, and then is heated to 650-720 ℃, and then enters the cathode of the solid oxide fuel cell together.
7. The power generation process as claimed in claim 5 or 6, wherein the temperature of the anode tail gas generated by the solid oxide fuel cell is 700-900 ℃, the anode tail gas enters the third heat exchanger through the anode tail gas output pipeline, the mixed gas output by the pre-reformer and the third heat exchanger exchange heat to reduce the temperature to 300-500 ℃, the fuel supplied is sequentially preheated by the second heat exchanger and the first heat exchanger step by step, the temperature is reduced to 60-200 ℃, and the fuel is mixed with a path of air and then enters the catalytic oxidation combustor together to enable the anode tail gas to be fully combusted.
8. The power generation process as claimed in claim 7, wherein the temperature of the anode tail gas generated by the solid oxide fuel cell is 750-850 ℃, the anode tail gas enters the third heat exchanger through the anode tail gas output pipeline, the mixed gas output by the prereformer and the third heat exchanger exchanges heat and cools to 300-500 ℃, the fuel supplied by the second heat exchanger and the first heat exchanger is preheated step by step in sequence, the temperature is reduced to 60-100 ℃, and then the fuel is mixed with a path of air and then enters the catalytic oxidation burner together, so that the anode tail gas is fully combusted.
9. The power generation process according to claim 5 or 6, wherein the fuel in step (1) is pipeline gas consisting of CO21-2V％、CH490-95V％、N21-3V％、C2H63-5V％、C3H80.8-2V％、C3H60.2-0.5V％。
10. The power generation process according to claim 5 or 6, wherein the composition of the mixed gas in step (1) is H2、CO、CO2And H2O, the water-carbon ratio is 1-5: 1.
11. the power generation process of claim 10 wherein the water to carbon ratio is 2-4: 1.
12. the power generation process according to claim 5 or 6, wherein the pressure of the cathode tail gas in the step (2) is increased to 150-400KPa after being pressurized by the recycle compressor.
13. The power generation process of claim 12 wherein the pressure is increased to 180 and 300 KPa.
14. The power generation process according to claim 5 or 6, wherein the saturated steam generated in the first and second steam generators in the step (2) has a temperature of 120 ℃ and a pressure of 300 ℃ and a pressure of 600 kPa.
15. The power generation process as claimed in claim 14, wherein the saturated steam generated in the first and second steam generators in step (2) has a temperature of 140-.
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