Combustor and hydrogen-doped combustion and carbon capture system of natural gas hydrogen-doped power plant

Abstract

The invention relates to the technical field of natural gas hydrogen-doped power plants, and discloses a combustor and a hydrogen-doped combustion and carbon capture system of the natural gas hydrogen-doped power plant, the combustor comprises a pipe body, the upstream of the airflow direction in the pipe body is defined as the front end, the downstream of the airflow direction is defined as the rear end, and the pipe body comprises a first mixing section, a second mixing section and a third mixing section which are sequentially communicated from the front end to the rear end; the two gases form hedging in the first mixing section to form premixed gas; an air flow speed is accelerated and then decelerated through a gradually-shrinking-gradually-expanding structure of the second mixing section, a low-pressure area is formed at the position of the minimum cross section, at the moment, air is introduced through a third air inlet, rapid air suction is achieved through pressure difference, the air and premixed gas are subjected to secondary dynamic mixing, and secondary mixed gas is formed; and after the secondarily mixed gas enters the third mixing section, the spoiler rotates under the driving of the gas flow to generate vortex, so that the mixing uniformity of the three gases is further enhanced, and the mixing uniformity is remarkably improved.

Description

Technical Field

[0001] The present invention relates to the technical field of natural gas hydrogen-blended power plants, and in particular to a burner, a hydrogen-blended combustion and carbon capture system for a natural gas hydrogen-blended power plant. Background Art

[0002] Hydrogen is a clean, efficient, and zero-carbon energy carrier with applications in various sectors, including transportation, industry, and power generation. Meanwhile, natural gas, as a relatively mature fossil fuel, still holds a crucial position in the energy mix. By blending a certain percentage of hydrogen into natural gas for combustion, carbon emissions can be reduced while also improving combustion characteristics and efficiency. Based on this technology, natural gas-hydrogen blended power plants have been developed, providing a platform for the large-scale utilization of hydrogen while generating electricity.

[0003] However, hydrogen molecules have a small mass and a higher average rate of molecular thermal motion at the same temperature. When entering the mixing section of the burner, hydrogen molecules will mix with air faster than methane molecules, resulting in uneven spatial distribution of hydrogen molecules and methane molecules in the combustion zone, and uneven distribution of oxygen in the mixed fuel, causing some fuel to not be completely burned, which in turn leads to lower overall combustion efficiency. Summary of the Invention

[0004] The technical problem to be solved by the present invention is that in the existing natural gas hydrogen-blended burner, hydrogen molecules and methane molecules are not mixed evenly, resulting in low combustion efficiency.

[0005] In order to solve the above technical problems, the present invention provides a burner, comprising a tube body, wherein the upstream of the airflow direction in the tube body is defined as the front end, and the downstream of the airflow direction in the tube body is defined as the rear end, and the tube body comprises a first mixing section, a second mixing section, and a third mixing section connected in sequence from the front end to the rear end;

[0006] At least one first air inlet is provided at the middle of the front end of the first mixing section, and at least two second air inlets are provided at intervals in the circumferential direction on the side wall of the first mixing section;

[0007] The size of the second mixing section gradually decreases and then increases from the front end to the rear end, and at least one third air inlet is provided on the side wall where the size of the second mixing section is the smallest;

[0008] A spoiler is provided in the third mixing section. The spoiler rotates around the axis of the third mixing section under the drive of the airflow to enhance the uniformity of gas mixing.

[0009] Preferably, the second mixing section includes a first contraction section, a first straight section and a first expansion section sequentially connected from the front end to the rear end;

[0010] The inner diameter of the first contraction section gradually decreases from the front end to the rear end, the inner diameter of the first straight section remains constant, a third air inlet is provided on the side wall of the first straight section, and the inner diameter of the first expansion section gradually increases from the front end to the rear end;

[0011] The third air inlet is arranged on the side wall of the first straight section.

[0012] Preferably, the spoiler is a spiral guide blade, the pitch of the spiral guide blade is 50 mm to 80 mm, and the inclination angle of the spiral guide blade is 45 degrees.

[0013] Preferably, the burner further comprises a combustion stabilization section and a combustion chamber, the rear end of the third mixing section is communicated with the front end of the combustion stabilization section, and the rear end of the combustion stabilization section is communicated with the combustion chamber;

[0014] The size of the stable combustion section gradually decreases and then increases from the front end to the rear end.

[0015] Preferably, the combustion stabilization section includes a second contraction section, a second straight section, and a second expansion section which are sequentially connected from the front end to the rear end;

[0016] The inner diameter of the second contraction section gradually decreases from the front end to the rear end, the inner diameter of the second straight section remains constant, and the inner diameter of the second expansion section gradually increases from the front end to the rear end.

[0017] Preferably, a combustion stabilizing plate is provided at the rear end of the combustion stabilizing section, and at least one air outlet is provided on the combustion stabilizing plate.

[0018] Compared with the prior art, a burner according to an embodiment of the present invention has the following advantages: the first mixing section of the embodiment of the present invention adopts central and circumferential multi-point air intake, hydrogen (or methane) is injected through the first air inlet in the middle of the front end, and methane (or hydrogen) enters from the second air inlet distributed circumferentially. The two gases collide in the first mixing section, and the collision and shear effect of the airflow achieve initial rapid mixing of the two gases to form a premixed gas;

[0019] The converging-diverging structure of the second mixing section accelerates the airflow first and then decelerates, forming a low-pressure area at the minimum cross-section. At this point, air is introduced through the third air inlet, and the pressure difference is used to achieve rapid air intake. The air is then dynamically mixed with the premixed gas to form a secondary mixed gas.

[0020] After the two mixed gases enter the third mixing section, the spoiler rotates driven by the airflow, generating vortices, which further enhance the mixing uniformity of the three gases and significantly improve the mixing uniformity.

[0021] The present invention also provides a hydrogen-blended combustion and carbon capture system for a natural gas hydrogen-blended power plant, comprising a hydrogen-blended combustion unit, a carbon fixation unit, a hydrogen production unit, a methane production unit, a flue gas transmission pipeline, a carbon dioxide transmission pipeline, an oxygen transmission pipeline, and a hydrogen transmission pipeline;

[0022] The burner of the hydrogen-blended combustion unit has a flue gas outlet at the rear end;

[0023] The carbon fixation unit includes a filter, a first heat exchanger, and a porous electrode. The filter is used to desulfurize the flue gas. The first heat exchanger is used to reduce the temperature of the flue gas after desulfurization. The first heat exchanger has a first outlet and a second outlet. An anion exchange membrane is provided in the porous electrode to separate the porous electrode into a cathode reaction chamber and an anode reaction chamber.

[0024] The flue gas outlet and the filter, the filter and the first heat exchanger, the first outlet and the cathode reaction chamber, and the second outlet and the hydrogen production unit are all connected through a flue gas delivery pipeline;

[0025] The cathode reaction chamber is connected to the methane production unit through a carbon dioxide transmission pipeline, and the anode reaction chamber is connected to the hydrogen production unit through an oxygen transmission pipeline;

[0026] The hydrogen production unit is used to prepare water molecules into hydrogen molecules and oxygen molecules;

[0027] The hydrogen production unit and the methane production unit are connected via a hydrogen transmission pipeline so that hydrogen molecules are transmitted to the methane production unit;

[0028] The methane production unit is used to produce methane molecules and water molecules from carbon dioxide molecules and hydrogen molecules.

[0029] Preferably, the hydrogen production unit includes a first reaction chamber and an electrolyzer, and the second outlet is connected to the first reaction chamber;

[0030] The first reaction chamber is used to prepare water molecules from the residual hydrogen molecules in the flue gas and the oxygen molecules generated in the anode reaction chamber;

[0031] The electrolyzer is used to electrolyze water molecules to generate oxygen molecules and hydrogen molecules.

[0032] Preferably, the hydrogen-blended combustion and carbon capture system of the natural gas-hydrogen-blended power plant further includes a first power generation unit and a second power generation unit;

[0033] The first power generation unit includes a solid-state battery, which is arranged at the outlet of the heat exchanger and is used to absorb heat from high-temperature flue gas to generate electricity;

[0034] The second power generation unit includes a second heat exchanger, a water source heat pump, a regeneration tower, a steam turbine and a generator connected in sequence;

[0035] The second heat exchanger includes a shell, a first heat exchange tube, a second heat exchange tube, and a circulation pump. The circulation pump drives the heat exchange medium in the first heat exchange tube and the second heat exchange tube to circulate, respectively. One end of the first heat exchange tube and the second heat exchange tube are both arranged in the shell so that the first heat exchange tube and the second heat exchange tube exchange heat in the shell. The other end of the first heat exchange tube is wrapped around the outer wall of the carbon dioxide delivery pipeline, and the other end of the second heat exchange tube is wrapped around the outer wall of the water source heat pump.

[0036] The water source heat pump provides thermal energy to the regeneration tower, generating high-temperature and high-pressure steam in the regeneration tower. The steam turbine is connected to the steam outlet of the regeneration tower, receiving steam power and outputting mechanical energy. The generator is mechanically connected to the output shaft of the steam turbine to convert the mechanical energy into electrical energy.

[0037] Preferably, it further comprises an intelligent control system, the intelligent control system comprises a controller, a first electrically controlled valve is provided on the first outlet, and a second electrically controlled valve is provided on the second outlet;

[0038] The controller is electrically connected to the first electrically controlled valve and is used to control the opening of the first electrically controlled valve;

[0039] The controller is electrically connected to the second electrically controlled valve and is used to control the opening of the second electrically controlled valve.

[0040] Compared with the prior art, the hydrogen-blended combustion and carbon capture system for a natural gas-hydrogen-blended power plant according to the embodiment of the present invention has the following beneficial effects:

[0041] The gas after hydrogen-mixed combustion has a high temperature and contains many impurities such as sulfide. In order to collect the carbon dioxide in the flue gas discharged from the flue gas outlet, the flue gas is first desulfurized by a filter, and then the temperature of the desulfurized flue gas is reduced by the first heat exchanger. A part of the desulfurized and cooled gas enters the cathode reaction chamber of the porous electrode. Under the action of a 5V-10V pulse electric field, CO2 accepts electrons (e - ) is reduced to CO and releases oxygen ions (O 2 -), achieving directional CO2 adsorption, with an adsorption capacity of 500 mg per gram of electrode. The anion exchange membrane is used to block the gas and allow oxygen ions to pass through. The oxygen ions migrate through the anion exchange membrane to the anode reaction chamber, where they lose electrons to generate O2 molecules.

[0042] The anode reaction chamber is connected to the hydrogen production unit through an oxygen delivery pipeline, so that the oxygen molecules generated in the anode reaction chamber are transported to the hydrogen production unit, and a part of the gas after desulfurization and cooling also enters the hydrogen production unit. A part of unburned hydrogen molecules remains in the gas after desulfurization and cooling. A catalytic device is set in the hydrogen production unit. Under the action of the catalyst, hydrogen molecules and oxygen molecules combine to generate water molecules, and then the water molecules are electrolyzed in the hydrogen production unit to generate higher purity hydrogen molecules.

[0043] After the porous electrode absorbs enough carbon monoxide, the reaction direction is switched by reverse pulse power supply, and the reverse reaction in the anode reaction chamber is: O2 is oxidized to oxygen ions (O 2 -); the reverse reaction in the cathode reaction chamber, oxygen ions (O 2 -) migrate to the cathode and combine with CO to regenerate CO2.

[0044] The cathode reaction chamber is connected to the methane production unit through a carbon dioxide transmission pipeline, so that the high-purity carbon dioxide generated by the reverse pulse in the cathode reaction chamber is transported to the methane production unit. At the same time, the hydrogen production unit and the methane production unit are connected through a hydrogen transmission pipeline, and the high-purity hydrogen molecules generated in the hydrogen production unit are also transported to the methane production unit. The methane production unit is used to prepare carbon dioxide molecules and hydrogen molecules into methane molecules and water molecules.

[0045] Direct carbon emissions are reduced by hydrogen-blended combustion, the CO2 capture rate in flue gas is improved by electrochemical carbon capture, and the CO2 and residual H2 in the flue gas are directionally converted into CO / CH4, realizing the recycling of carbon resources and significantly improving the efficiency of energy cascade utilization. BRIEF DESCRIPTION OF THE DRAWINGS

[0046] Figure 1 Schematic diagram of the tube structure of a burner according to an embodiment of the present invention;

[0047] Figure 2 yes Figure 1 AA sectional view;

[0048] Figure 3 yes Figure 1 BB cross-sectional view;

[0049] Figure 4 This is a flow chart of a hydrogen-blended combustion and carbon capture system for a natural gas-hydrogen-blended power plant according to an embodiment of the present invention.

[0050] In the figure, 1, first mixing section, 2, second mixing section, 21, first contraction section, 22, first straight section, 23, first expansion section, 3, third mixing section, 30, rotating shaft, 4, combustion stabilization section, 41, second contraction section, 42, second straight section, 43, second expansion section, 5, first air inlet, 51, hydrogen nozzle, 6, second air inlet, 61, methane nozzle, 7, third air inlet, 8, spiral guide vane, 9, combustion stabilization plate, 10, air outlet, 11, flue gas outlet, 12, Filter, 13. First heat exchanger, 131. First outlet, 132. Second outlet, 14. Porous electrode, 141. Cathode reaction chamber, 142. Anion exchange membrane, 143. Anode reaction chamber, 15. First reaction chamber, 16. Electrolyzer, 17. Second reaction chamber, 18. Solid-state battery, 19. Second heat exchanger, 20. Water source heat pump, 21. Regeneration tower, 22. Steam turbine, 23. Generator, 24. Third heat exchanger, 25. First electric-controlled valve, 26. Second electric-controlled valve. DETAILED DESCRIPTION

[0051] The following embodiments of the present invention are described in further detail with reference to the accompanying drawings and examples. The following examples are used to illustrate the present invention but are not intended to limit the scope of the present invention.

[0052] In the description of the present invention, it should be understood that the terms "center", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or position relationship, are based on the orientation or position relationship shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention.

[0053] It should be understood that, while the present invention uses terms such as "first" and "second" to describe various types of information, such information should not be limited to these terms; these terms are merely used to distinguish information of the same type from one another. For example, "first" information could also be referred to as "second" information, and similarly, "second" information could also be referred to as "first" information without departing from the scope of the present invention.

[0054] In the description of the present invention, it should be noted that, unless otherwise expressly specified or limited, the terms "mounted," "connected," and "connected" should be understood in a broad sense. For example, they may refer to fixed, detachable, or integral connections; mechanical or electrical connections; direct or indirect connections through an intermediate medium; and internal communication between two components. Those skilled in the art will understand the specific meanings of the above terms in the present invention based on the specific circumstances.

[0055] like Figures 1 to 3 As shown, a burner according to a preferred embodiment of the present invention includes a tube body, wherein the upstream of the airflow direction in the tube body is defined as the front end, and the downstream of the airflow direction in the tube body is defined as the rear end, and the tube body includes a first mixing section 1, a second mixing section 2, and a third mixing section 3 connected in sequence from the front end to the rear end;

[0056] At least one first air inlet 5 is provided in the middle of the front end of the first mixing section 1, and at least two second air inlets 6 are provided at intervals along the circumference of the side wall of the first mixing section 1;

[0057] The size of the second mixing section 2 gradually decreases and then increases from the front end to the rear end, and at least one third air inlet 7 is provided on the side wall of the second mixing section 2 where the size is the smallest;

[0058] A spoiler is provided in the third mixing section 3. The spoiler rotates around the axis of the third mixing section 3 under the drive of the airflow to enhance the uniformity of gas mixing.

[0059] The first mixing section 1 of the embodiment of the present invention adopts central and circumferential multi-point air intake. Hydrogen (or methane) is injected through the first air inlet in the middle of the front end, and methane (or hydrogen) enters from the second air inlet 6 distributed circumferentially. The two gases form a collision in the first mixing section 1, and the two gases are initially and rapidly mixed by airflow collision and shear effect to form a premixed gas.

[0060] The gradually converging and expanding structure of the second mixing section 2 causes the airflow velocity to first accelerate and then decelerate, forming a low-pressure area at the minimum cross-section. At this time, air is introduced through the third air inlet 7, and the pressure difference is used to achieve rapid air inhalation, and the air is dynamically mixed with the premixed gas for a second time to form a secondary mixed gas.

[0061] After the two mixed gases enter the third mixing section 3, the spoiler rotates under the drive of the airflow, generating a vortex, further enhancing the mixing uniformity of the three gases and significantly improving the mixing uniformity.

[0062] Specifically, the second mixing section 2 includes a first contraction section 21, a first straight section 22 and a first expansion section 23 which are sequentially connected from the front end to the rear end;

[0063] The inner diameter of the first contraction section 21 gradually decreases from the front end to the rear end, the inner diameter of the first straight section 22 remains constant, a third air inlet 7 is provided on the side wall of the first straight section 22, and the inner diameter of the first expansion section 23 gradually increases from the front end to the rear end;

[0064] The third air inlet 7 is provided on the side wall of the first straight section 22 .

[0065] A first straight section 22 with a constant inner diameter is provided between the first contraction section 21 and the first expansion section 23, so that a stable low-pressure area is formed in the first straight section 22. A third air inlet 7 is provided on the side wall of the first straight section 22, thereby improving the stability of air intake.

[0066] Specifically, the diameter of the first straight section 22 is 15 mm, thereby ensuring that the flow rate of the mixed gas in the first straight section 22 is stably controlled at 20 m / s to 30 m / s, effectively avoiding the occurrence of backfire and ensuring the safety and stability of the premixing process.

[0067] Specifically, the spoiler is a spiral guide blade 8, the pitch of the spiral guide blade 8 is 50mm to 80mm, and the inclination angle of the spiral guide blade 8 is 45 degrees; a rotating shaft 30 is provided in the tube body, and a bearing seat is provided on the tube wall at the rear end of the tube body, and a bearing is provided in the bearing seat. The rear end of the rotating shaft 30 is fixedly connected to the inner ring of the bearing, and the front end of the rotating shaft 30 is cantilevered into the third mixing section 3. The spiral guide blade 8 is fixedly mounted on the rotating shaft 30, and the spiral guide blade 8 is dynamically rotated by the rotating shaft 30. When the mixed gas flows through the spiral guide blade 8, the airflow impacts the inclination angle of the spiral guide blade 8 to generate a tangential torque to drive the rotating shaft 30 to rotate. During the rotation process, the spiral structure of the spiral guide blade 8 converts the axial airflow into a high-intensity spiral vortex, thereby realizing uniform mixing of the three gases.

[0068] Specifically, the thickness of the spiral guide blade 8 is 2 mm, ensuring that the spiral guide blade 8 has sufficient structural strength.

[0069] Specifically, the burner further includes a stable combustion section 4 and a combustion chamber, the rear end of the third mixing section 3 is connected to the front end of the stable combustion section 4, and the rear end of the stable combustion section 4 is connected to the combustion chamber;

[0070] The size of the combustion stabilization section 4 gradually decreases and then increases from the front end to the rear end.

[0071] The gradually converging and diverging flow passage of the combustion stabilization section 4 further accelerates the mixed gas at the minimum cross-section, significantly shortening the residence time of the mixed fuel in the third mixing section 3 and achieving rapid and complete combustion of the hydrogen-blended mixed gas.

[0072] Specifically, the combustion stabilization section 4 includes a second contraction section 41, a second straight section 42 and a second expansion section 43 connected in sequence from the front end to the rear end;

[0073] The inner diameter of the second contraction section 41 gradually decreases from the front end to the rear end, the inner diameter of the second straight section 42 remains constant, and the inner diameter of the second expansion section 43 gradually increases from the front end to the rear end.

[0074] The diameter of the second straight section 42 is 25 mm, and the rear end diameter of the second expansion section 43 is 35 mm, with a contraction ratio of 1.5:1. The throat contraction design of the Laval nozzle can increase the speed of the combustion gas to 50 m / s, which not only speeds up the combustion speed but also effectively suppresses the generation of NOx, reducing the NOx emission concentration to ≤30 mg / m 3 , meeting strict environmental protection requirements.

[0075] Specifically, a combustion stabilizing plate 9 is provided at the rear end of the combustion stabilizing section 4 , and at least one air outlet 10 is provided on the combustion stabilizing plate 9 .

[0076] The combustion stabilizing plate 9 is made of 316L stainless steel, the aperture of the air outlet 10 is set to 3mm to 5mm, and the opening rate of the air outlet 10 is 30%. The function of the combustion stabilizing plate 9 is to form a local low-speed zone at the burner outlet, so that the flame can be stably attached here to avoid the occurrence of flame deignition.

[0077] The working process of the burner provided by the embodiment of the present invention is as follows:

[0078] Hydrogen (or methane) is injected through the first air inlet in the middle of the front end, and methane (or hydrogen) enters from the second air inlet 6 evenly distributed around the side wall of the first mixing section 1. The two gases form counter-jet flows in the first mixing section 1, and rapid mixing is achieved through airflow collision and shear effects.

[0079] The premixed gas enters the second mixing section 2 and passes through the first contraction section 11, the first straight section 12, and the first expansion section 13 in sequence. The airflow is accelerated in the first contraction section 11. After entering the first straight section 12, the flow velocity stabilizes, forming a local low-pressure area in the first straight section 12. The third air inlet 7 is provided on the side wall of the first straight section 12. The third air inlet 7 utilizes the pressure difference between the low-pressure area and atmospheric pressure to draw air in at high speed through the Venturi effect. The air and the premixed gas form radial convection in the first straight section 12, completing secondary mixing and forming a secondary mixed gas.

[0080] After the secondary mixed gas enters the third mixing section 3, it impacts the 45-degree inclined surface of the spiral guide vanes 8. The tangential torque of the airflow and the vanes drives the shaft to rotate. The cantilevered fixed vanes at the front end of the shaft convert the axial airflow into a high-intensity spiral vortex, further enhancing the mixing uniformity of the three gases through centrifugal force.

[0081] The mixed gas enters the stable combustion section 4, and passes through the second contraction section 41, the second straight section 42 and the second expansion section 43 in sequence. In the second contraction section 41, the airflow is accelerated to 50m / s, and then decelerated and pressurized after entering the second expansion section 43. The high-speed airflow shortens the mixing time of the fuel and air. The stable combustion plate 9 is made of 316L stainless steel with an opening rate of 30%, forming a local low-speed zone at the entrance of the combustion chamber, so that the flame can be stably attached here to avoid the occurrence of flame deignition.

[0082] In summary, the embodiment of the present invention provides a burner in which the first mixing section of the burner adopts central and circumferential multi-point air intake. Hydrogen (or methane) is injected through the first air inlet in the middle of the front end, and methane (or hydrogen) enters from the second air inlet distributed circumferentially. The two gases form a collision in the first mixing section, and the two gases are initially and rapidly mixed by airflow collision and shear effect to form a premixed gas.

[0083] The converging-diverging structure of the second mixing section accelerates the airflow first and then decelerates, forming a low-pressure area at the minimum cross-section. At this point, air is introduced through the third air inlet, and the pressure difference is used to achieve rapid air intake. The air is then dynamically mixed with the premixed gas to form a secondary mixed gas.

[0084] After the two mixed gases enter the third mixing section, the spoiler rotates driven by the airflow, generating vortices, which further enhance the mixing uniformity of the three gases and significantly improve the mixing uniformity.

[0085] like Figure 4 As shown, the present application also provides a hydrogen-blended combustion and carbon capture system for a natural gas hydrogen-blended power plant, comprising a hydrogen-blended combustion unit, a carbon fixation unit, a hydrogen production unit, a methane production unit, a flue gas transmission pipeline, a carbon dioxide transmission pipeline, an oxygen transmission pipeline, and a hydrogen transmission pipeline;

[0086] The hydrogen-blended combustion unit comprises the above-mentioned burner, and the rear end of the burner has a flue gas outlet 11;

[0087] The carbon fixation unit includes a filter 12, a first heat exchanger 13, and a porous electrode 14. The filter 12 is used to desulfurize the flue gas. The first heat exchanger 13 is used to reduce the temperature of the flue gas after desulfurization. The first heat exchanger 13 has a first outlet 131 and a second outlet 132. An anion exchange membrane 142 is provided in the porous electrode 14 to separate the porous electrode 14 into a cathode reaction chamber 141 and an anode reaction chamber 143.

[0088] The flue gas outlet 11 and the filter 12, the filter 12 and the first heat exchanger 13, the first outlet 131 and the cathode reaction chamber 141, and the second outlet 132 and the hydrogen production unit are all connected through flue gas delivery pipelines;

[0089] The cathode reaction chamber 141 is connected to the methane production unit via a carbon dioxide delivery pipeline, and the anode reaction chamber 143 is connected to the hydrogen production unit via an oxygen delivery pipeline;

[0090] The hydrogen production unit and the methane production unit are connected via a hydrogen transmission pipeline;

[0091] The hydrogen production unit is used to prepare water molecules into hydrogen molecules and oxygen molecules;

[0092] The methane production unit is used to produce methane molecules and water molecules from carbon dioxide molecules and hydrogen molecules.

[0093] The gas after hydrogen-mixed combustion has a high temperature and contains many impurities such as sulfides. In order to collect carbon dioxide in the flue gas discharged from the flue gas outlet 11, the flue gas is first desulfurized by the filter 12, and then the temperature of the desulfurized flue gas is reduced by the first heat exchanger 13. A part of the desulfurized and cooled gas enters the cathode reaction chamber 141 of the porous electrode 14. Under the action of the 5V-10V pulse electric field, CO2 accepts electrons (e) through electrochemical reaction in the cathode reaction chamber 141. - ) is reduced to CO and releases oxygen ions (O 2 -), reaction formula:

[0094] CO2+2e - →CO+O 2 -

[0095] Achieve directional adsorption of CO2, with an adsorption capacity of 500 mg per gram of electrode. The anion exchange membrane 142 is used to block gas and allow oxygen ions to pass through. The oxygen ions migrate through the anion exchange membrane 142 to the anode reaction chamber 143, where they lose electrons to generate O2 molecules. The reaction formula is:

[0096] 2O 2 --4e - →O2

[0097] The anode reaction chamber 143 is connected to the hydrogen production unit through an oxygen delivery pipeline, so that the oxygen molecules generated in the anode reaction chamber 143 are transported to the hydrogen production unit, and a part of the gas after desulfurization and cooling also enters the hydrogen production unit. A part of unburned hydrogen molecules remains in the gas after desulfurization and cooling. A catalytic device is set in the hydrogen production unit. Under the action of the catalyst, hydrogen molecules and oxygen molecules combine to generate water molecules, and then the water molecules are electrolyzed in the hydrogen production unit to generate hydrogen molecules with higher purity.

[0098] After the porous electrode 14 absorbs enough carbon monoxide, the reverse pulse power supply switches the reaction direction, and the reverse reaction in the anode reaction chamber 143 is: O2 is oxidized to oxygen ions (O 2 -), reaction formula:

[0099] O2+4e - →2O 2 -

[0100] The reverse reaction in the cathode reaction chamber 141: oxygen ions (O 2 -) migrates to the cathode and combines with CO to regenerate CO2, reaction formula:

[0101] CO+O 2 --2e - →CO2

[0102] The cathode reaction chamber 141 is connected to the methane production unit through a carbon dioxide delivery pipeline, so that the high-purity carbon dioxide generated by the reverse pulse in the cathode reaction chamber 141 is delivered to the methane production unit. At the same time, the hydrogen production unit and the methane production unit are connected through a hydrogen delivery pipeline, and the high-purity hydrogen molecules generated in the hydrogen production unit are also delivered to the methane production unit. The methane production unit is used to prepare carbon dioxide molecules and hydrogen molecules into methane molecules and water molecules.

[0103] Direct carbon emissions are reduced by hydrogen-blended combustion, the CO2 capture rate in flue gas is improved by electrochemical carbon capture, and the CO2 and residual H2 in the flue gas are directionally converted into CO / CH4, realizing the recycling of carbon resources and significantly improving the efficiency of energy cascade utilization.

[0104] Specifically, the filter includes three layers of ceramic membranes. The pore size of each layer of ceramic membrane gradually decreases from upstream to downstream in the direction of air flow. The surface layer is a fine filter layer with a pore size of 0.1μm, which can effectively intercept particles with a particle size greater than 0.1μm and achieve a dust removal efficiency of 99%; the middle layer is a transition layer with a pore size of 1μm-5μm; the bottom layer is a support layer with a pore size of 10μm-20μm.

[0105] During the preparation of ceramic membranes, nano-sized zinc oxide (ZnO) and calcium oxide (CaO) particles are uniformly loaded onto the inner wall of the membrane pores through an impregnation-sintering process, with a loading of 5wt%-10wt%. These alkaline metal oxides can react chemically with acidic gases such as HCl and HF. For example, zinc oxide reacts with HCl to form zinc chloride and water, using the following reaction formula:

[0106] ZnO+2HCl→ZnCl2+H2O

[0107] Calcium oxide reacts with HF to produce calcium fluoride and water. The reaction formula is:

[0108] CaO + 2HF → CaF2 + H2O

[0109] Nanoparticles have a high specific surface area (50m 2 / g-100m 2 / g), which can provide a large number of reactive sites, so that the saturated adsorption capacity of the ceramic membrane for HCl and HF reaches 150 mg / g and 200 mg / g, respectively.

[0110] In addition, 0.1wt%-0.5wt% of copper oxide (CuO) catalyst is introduced into the ceramic membrane to form an "adsorption-catalysis" synergistic system. Copper oxide can accelerate the oxidation process of SO2. The reaction formula is:

[0111] 2SO2+O2→2SO3

[0112] The generated SO3 reacts with CaO to generate CaSO4, the reaction formula is:

[0113] SO3+CaO→CaSO4

[0114] This design significantly increases the SO2 removal efficiency of the ceramic membrane from 30% of simple physical adsorption to over 85%, achieving simultaneous and efficient purification of multiple acidic gases.

[0115] Through the above-mentioned structural and functional design, the filter of the present invention breaks through the limitation that traditional ceramic membranes can only physically intercept particulate matter, and realizes the integrated function of dust removal and acid gas adsorption, providing a clean gas source for subsequent solid or residual hydrogen in the flue gas, reducing the impact of acid gas on the system and extending the service life of the system.

[0116] Specifically, the first heat exchanger 13 includes a shell and tube heat exchanger. High-temperature flue gas containing pollutants such as sulfur dioxide (SO2) enters the air inlet of the shell and tube heat exchanger. At this time, the flue gas temperature is usually between 40°C and 60°C. The flue gas transfers heat to the 20°C cooling water flowing in the tube through the tube bundle wall. This indirect heat exchange method effectively avoids a series of problems that may be caused by the mixing of flue gas and cooling water, such as water pollution and equipment corrosion. Due to the large temperature difference between the flue gas and the cooling water, heat is quickly transferred from the flue gas to the cooling water, causing the flue gas temperature to drop rapidly.

[0117] As the flue gas temperature decreases, the water vapor within it gradually undergoes a phase change, transforming from gas to liquid, forming small water droplets. During this process, sulfur dioxide (SO2) has a certain degree of water solubility and dissolves in these condensed water droplets. Furthermore, according to Henry's law, a decrease in temperature increases the solubility of sulfur dioxide in water, further promoting the absorption of SO2. A gas-liquid separation device is integrated at the tail end of the shell-and-tube heat exchanger. After cooling and condensing, the flue gas carries a large number of small water droplets containing SO2 and enters the gas-liquid separation device. The gas-liquid separation device utilizes efficient cyclone separation technology, utilizing centrifugal force to separate the water droplets from the flue gas. The SO2 concentration in the separated clean flue gas can be reduced to ≤10ppm, and then discharged through the first outlet 131 and the second outlet 132, respectively, providing a clean gas source for subsequent processes. The separated sulfur-containing wastewater is collected through a dedicated pipeline and transported to a subsequent wastewater treatment unit for centralized treatment, ensuring that the entire process meets environmental protection requirements.

[0118] Specifically, the hydrogen production unit includes a first reaction chamber 15 and an electrolyzer 16, and the second outlet 132 is connected to the first reaction chamber 15;

[0119] The reaction chamber is used to prepare water molecules from the residual hydrogen molecules in the flue gas and the oxygen molecules generated in the anode reaction chamber 143;

[0120] The electrolytic cell 16 is used to electrolyze water molecules to generate oxygen molecules and hydrogen molecules.

[0121] Specifically, the first reaction chamber 15 is filled with a noble metal-based catalyst (such as Pt / Al2O3 or Pd / CeO2). At room temperature to 150°C and normal pressure, H2 and O2 undergo redox reaction on the surface of the noble metal-based catalyst, as shown in the following reaction formula:

[0122] 2H2+O2→2H2O

[0123] The synthetic water is electrolyzed into H2 and O2 in the electrolytic cell 16, thereby purifying the low-concentration hydrogen molecules remaining in the flue gas. High-purity hydrogen molecules are generated in the electrolytic cell 16, providing high-purity raw materials for the downstream methane production unit.

[0124] Specifically, the methane production unit includes a second reaction chamber 17, which is filled with a Ni-based catalyst. The captured CO2 and the H2 generated by electrolysis synthesize CH4 under the action of the Ni-based catalyst (400°C, 3MPa). The reaction formula is:

[0125] CO2+4H2→CH4+2H2O

[0126] Specifically, the hydrogen blending combustion and carbon capture system of the natural gas hydrogen blending power plant further includes a first power generation unit and a second power generation unit;

[0127] The first power generation unit includes a solid-state battery 18, which is arranged at the outlet of the heat exchanger and is used to absorb heat from high-temperature flue gas to generate electricity;

[0128] The second power generation unit includes a second heat exchanger 19, a water source heat pump 20, a regeneration tower 21, a steam turbine 22, and a generator 23 connected in sequence;

[0129] The second heat exchanger 19 includes a shell, a first heat exchange tube, a second heat exchange tube, and a circulation pump. The circulation pump drives the heat exchange medium in the first heat exchange tube and the second heat exchange tube to circulate. One end of the first heat exchange tube and the second heat exchange tube are both arranged in the shell so that the first heat exchange tube and the second heat exchange tube exchange heat in the shell. The other end of the first heat exchange tube is wrapped around the outer wall of the carbon dioxide delivery pipeline, and the other end of the second heat exchange tube is wrapped around the outer wall of the water source heat pump 20.

[0130] The water source heat pump 20 provides thermal energy to the regeneration tower 21, generating high-temperature and high-pressure steam in the regeneration tower 21. The steam turbine 22 is connected to the steam outlet of the regeneration tower 21, receives steam power and outputs mechanical energy. The generator 23 is mechanically connected to the output shaft of the steam turbine 22 to convert the mechanical energy into electrical energy.

[0131] The solid-state battery 18 directly converts the waste heat of high-temperature flue gas into electrical energy, simplifying the energy conversion path. The water source heat pump 20 provides heat energy for the regeneration tower 21. At the same time, the second heat exchanger 19 surrounds the carbon dioxide transmission pipeline to recover the heat released during the carbon dioxide regeneration process, reducing the energy consumption of the water source heat pump 20, achieving the dual functions of industrial waste heat power generation and carbon neutrality, and improving the energy utilization efficiency of the power plant.

[0132] Specifically, the hydrogen-blended combustion and carbon capture system of the natural gas hydrogen-blended power plant also includes a third heat exchanger 24 and a heat energy transmission pipeline. The regeneration tower 21 and the burner are connected through the heat energy transmission pipeline. The third heat exchanger 24 is arranged on the heat energy transmission pipeline, and a portion of the heat energy is directionally transmitted to the air inlet end of the burner through the heat energy transmission pipeline for preheating the hydrogen, methane and air mixture, thereby reducing the activation energy requirement of the combustion reaction and improving the combustion efficiency.

[0133] Specifically, the first heat exchange tube releases adsorption heat (about 40kJ / molCO2) during the CO2 desorption stage and transfers it to the water source heat pump through the second heat exchange tube. The water source heat pump is equipped with a refrigerant (such as R1233zd(E)), an evaporator and a compressor. The evaporator drives the refrigerant circulation. The refrigerant absorbs heat and vaporizes, and then is pressurized and heated to 90-100°C by the compressor. After heating, it enters the regeneration tower reboiler to release heat, heating the rich liquid to 80°C, which is significantly lower than the 120°C required by the traditional amine method. The water source heat pump operates with an energy efficiency ratio of COP=4.0, consuming 1kW of electricity to output 4kW of heat energy, saving 75% energy compared to traditional electric heating, reducing the heat consumption of the regeneration tower to 0.25kWh / kgCO2-0.35kWh / kgCO2, while the traditional amine method is 0.8kWh / kgCO2-1.2kWh / kgCO2, significantly reducing the overall energy consumption of the system. The 80℃ lean liquid waste heat discharged from the regeneration tower is cooled to 60℃-70℃ through the lean and rich liquid heat exchanger, and then divided into two cascade utilization. The waste heat is preheated from the normal temperature of 25℃ to 50℃-60℃ through the third heat exchanger 24, thereby improving combustion efficiency. The remaining waste heat drives the steam turbine 22 to generate electricity.

[0134] Specifically, it also includes an intelligent control system, which includes a controller, a first electrically controlled valve 25 is provided on the first outlet 131, and a second electrically controlled valve 26 is provided on the second outlet 132;

[0135] The controller is electrically connected to the first electrically controlled valve 25 and is used to control the opening of the first electrically controlled valve 25;

[0136] The controller is electrically connected to the second electrically controlled valve 26 and is used to control the opening of the second electrically controlled valve 26 .

[0137] The controller controls the distribution ratio of the desulfurized flue gas between the porous electrode 14 and the hydrogen production unit in real time by adjusting the opening of the first electrically controlled valve 25 and the second electrically controlled valve 26 .

[0138] Specifically, the intelligent control system also includes an intelligent carbon flow scheduling module and a blockchain carbon tracking system. The intelligent carbon flow scheduling module includes a reinforcement learning control algorithm (DQN), which collects 12-dimensional data such as CO2 concentration, H2 flow, and system pressure in real time, constructs a state vector xt = [xt1, xt2, ..., xtn] (n ≥ 12), and optimizes the electric valve opening and energy distribution through a deep Q network. The response time is < 100ms, and the capture efficiency fluctuation is ≤ ± 2%;

[0139] The blockchain carbon tracking system digitally hashes the captured CO2 and uploads the entire process data to the chain, making the carbon footprint traceable (with an accuracy of kg level) to meet carbon trading and regulatory needs.

[0140] The working process of the hydrogen-blended combustion and carbon capture system of the natural gas hydrogen-blended power plant provided by the embodiment of the present invention is as follows:

[0141] The burner mixes hydrogen and methane in proportion and burns them to generate high-temperature flue gas. The flue gas is discharged through the flue gas outlet 11 and then enters the filter 12 for desulfurization to remove sulfide impurities. The desulfurized flue gas enters the first heat exchanger 13 for cooling and is divided into two paths: one path enters the cathode reaction chamber 141 of the porous electrode 14 through the first electric control valve 25 to control the flow rate, and the other path is transported to the hydrogen production unit reaction chamber through the second electric control valve 26.

[0142] In the cathode reaction chamber 141 of the porous electrode 14, CO2 accepts electrons under a 5V-10V pulse electric field to generate carbon monoxide and oxygen ions, achieving directional adsorption of CO2. The oxygen ions migrate through the anion exchange membrane 142 to the anode reaction chamber 143 to generate O2.

[0143] The residual H2 in the flue gas at the second outlet 132 and the O2 generated in the anode reaction chamber 143 synthesize water under the action of the precious metal catalyst in the reaction chamber. The synthesized water is electrolyzed into high-purity H2 and O2 in the electrolytic cell 16. The H2 is transported to the methane production unit, and the O2 is recovered for combustion or hydrogen production.

[0144] After the porous electrode 14 adsorbs enough CO, the reaction direction is switched by a reverse pulse power supply, and the cathode reaction chamber 141 releases high-purity CO2, which is then transported to the methane production unit;

[0145] The methane production unit catalytically synthesizes CH4 from CO2 and electrolytic H2, and the methane is returned to the burner as fuel, forming a carbon-neutral cycle.

[0146] The solid-state battery 18 absorbs the waste heat from the flue gas at the outlet of the first heat exchanger 13 to directly generate electricity. The second heat exchanger 19 recovers the waste heat from the carbon dioxide transmission pipeline and transmits it to the water source heat pump 20. The water source heat pump 20 drives the regeneration tower 21 to generate high-pressure steam. The high-pressure steam drives the steam turbine 22 to generate electricity.

[0147] The third heat exchanger 24 transfers the waste heat from the regeneration tower 21 to the air inlet of the burner through a heat energy transfer pipeline, preheating the mixed gas and reducing the energy required for combustion.

[0148] The controller adjusts the opening of the first electrically controlled valve 25 and the second electrically controlled valve 26 in real time, dynamically distributes the flue gas flow direction, and ensures carbon capture efficiency, hydrogen production purity and combustion stability.

[0149] In summary, the embodiment of the present invention provides a hydrogen-blended combustion and carbon capture system for a natural gas hydrogen-blended power plant. The gas after hydrogen-blended combustion has a high temperature and contains a large number of impurities such as sulfides. In order to collect carbon dioxide in the flue gas discharged from the flue gas outlet, the flue gas is first desulfurized by a filter, and then the temperature of the desulfurized flue gas is reduced by a first heat exchanger. A portion of the desulfurized and cooled gas enters the cathode reaction chamber of the porous electrode. Under the action of a 5V-10V pulse electric field, CO2 accepts electrons (e- ) is reduced to CO and releases oxygen ions (O 2 -), achieving directional CO2 adsorption, with an adsorption capacity of 500 mg per gram of electrode. The anion exchange membrane is used to block the gas and allow oxygen ions to pass through. The oxygen ions migrate through the anion exchange membrane to the anode reaction chamber, where they lose electrons to generate O2 molecules.

[0150] The anode reaction chamber is connected to the hydrogen production unit through an oxygen delivery pipeline, so that the oxygen molecules generated in the anode reaction chamber are transported to the hydrogen production unit, and a part of the gas after desulfurization and cooling also enters the hydrogen production unit. A part of unburned hydrogen molecules remains in the gas after desulfurization and cooling. A catalytic device is set in the hydrogen production unit. Under the action of the catalyst, hydrogen molecules and oxygen molecules combine to generate water molecules, and then the water molecules are electrolyzed in the hydrogen production unit to generate higher purity hydrogen molecules.

[0151] After the porous electrode absorbs enough carbon monoxide, the reaction direction is switched by reverse pulse power supply, and the reverse reaction in the anode reaction chamber is: O2 is oxidized to oxygen ions (O 2 -); the reverse reaction in the cathode reaction chamber, oxygen ions (O 2 -) migrate to the cathode and combine with CO to regenerate CO2.

[0152] The cathode reaction chamber is connected to the methane production unit through a carbon dioxide transmission pipeline, so that the high-purity carbon dioxide generated by the reverse pulse in the cathode reaction chamber is transported to the methane production unit. At the same time, the hydrogen production unit and the methane production unit are connected through a hydrogen transmission pipeline, and the high-purity hydrogen molecules generated in the hydrogen production unit are also transported to the methane production unit. The methane production unit is used to prepare carbon dioxide molecules and hydrogen molecules into methane molecules and water molecules.

[0153] Direct carbon emissions are reduced by hydrogen-blended combustion, the CO2 capture rate in flue gas is improved by electrochemical carbon capture, and the CO2 and residual H2 in the flue gas are directionally converted into CO / CH4, realizing the recycling of carbon resources and significantly improving the efficiency of energy cascade utilization.

[0154] The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and substitutions can be made without departing from the technical principles of the present invention. These improvements and substitutions should also be regarded as the scope of protection of the present invention.

Claims

1. A burner, characterized in that The invention comprises a pipe body, wherein the upstream of the airflow direction in the pipe body is defined as the front end, and the downstream of the airflow direction is defined as the rear end, and the pipe body comprises a first mixing section (1), a second mixing section (2), and a third mixing section (3) which are sequentially connected from the front end to the rear end; At least one first air inlet (5) is provided at the middle of the front end of the first mixing section (1), and at least two second air inlets (6) are provided at intervals in the circumferential direction on the side wall of the first mixing section (1); The size of the second mixing section (2) gradually decreases and then gradually increases from the front end to the rear end, and at least one third air inlet (7) is provided on the side wall of the second mixing section (2) where the size is the smallest; A flow spoiler is provided in the third mixing section (3), and the flow spoiler rotates around the axis of the third mixing section (3) under the driving of the airflow to enhance the uniformity of gas mixing.

2. The burner according to claim 1, characterized in that The second mixing section (2) comprises a first contraction section (21), a first straight section (22) and a first expansion section (23) which are sequentially connected from the front end to the rear end; The inner diameter of the first contraction section (21) gradually decreases from the front end to the rear end, the inner diameter of the first straight section (22) remains constant, a third air inlet (7) is provided on the side wall of the first straight section (22), and the inner diameter of the first expansion section (23) gradually increases from the front end to the rear end; The third air inlet (7) is arranged on the side wall of the first straight section (22).

3. The burner according to claim 1, characterized in that The spoiler is a spiral guide blade (8), the pitch of the spiral guide blade (8) is 50 mm to 80 mm, and the inclination angle of the spiral guide blade (8) is 45 degrees.

4. The burner according to claim 1, characterized in that The burner further comprises a combustion stabilization section (4) and a combustion chamber, the rear end of the third mixing section (3) is communicated with the front end of the combustion stabilization section (4), and the rear end of the combustion stabilization section (4) is communicated with the combustion chamber; The size of the combustion stabilization section (4) gradually decreases and then gradually increases from the front end to the rear end.

5. The burner according to claim 4, characterized in that The combustion stabilization section (4) comprises a second contraction section (41), a second straight section (42) and a second expansion section (43) which are sequentially connected from the front end to the rear end; The inner diameter of the second contraction section (41) gradually decreases from the front end to the rear end, the inner diameter of the second straight section (42) remains constant, and the inner diameter of the second expansion section (43) gradually increases from the front end to the rear end.

6. The burner according to claim 4 or 5, characterized in that A combustion stabilizing plate (9) is provided at the rear end of the combustion stabilizing section (4), and at least one air outlet (10) is provided on the combustion stabilizing plate (9).

7. The hydrogen-combustion and carbon capture system of natural gas-combustion power plant is characterized by: It includes hydrogen blending combustion unit, carbon fixation unit, hydrogen production unit, methane production unit, flue gas transmission pipeline, carbon dioxide transmission pipeline, oxygen transmission pipeline and hydrogen transmission pipeline; The hydrogen-blended combustion unit comprises the burner according to any one of claims 1 to 6, wherein the rear end of the burner has a flue gas outlet (11); The carbon fixation unit comprises a filter (12), a first heat exchanger (13) and a porous electrode (14), wherein the filter (12) is used for desulfurizing flue gas, the first heat exchanger (13) is used for reducing the temperature of the flue gas after desulfurization, the first heat exchanger (13) has a first outlet (131) and a second outlet (132), and an anion exchange membrane (142) is provided in the porous electrode (14) to separate the porous electrode (14) into a cathode reaction chamber (141) and an anode reaction chamber (143); The flue gas outlet (11) and the filter (12), the filter (12) and the first heat exchanger (13), the first outlet (131) and the cathode reaction chamber (141), and the second outlet (132) and the hydrogen production unit are all connected through the flue gas delivery pipeline; The cathode reaction chamber (141) is connected to the methane production unit via the carbon dioxide delivery pipeline, and the anode reaction chamber (143) is connected to the hydrogen production unit via the oxygen delivery pipeline; The hydrogen production unit is used to prepare water molecules into hydrogen molecules and oxygen molecules; The hydrogen production unit and the methane production unit are connected via the hydrogen delivery pipeline so that the hydrogen molecules are transmitted to the methane production unit; The methane production unit is used to produce methane molecules and water molecules from carbon dioxide molecules and hydrogen molecules.

8. The natural gas hydrogen blended power plant hydrogen blended combustion and carbon capture system according to claim 7, characterized in that: The hydrogen production unit comprises a first reaction chamber (15) and an electrolyzer (16), and the second outlet (132) is in communication with the first reaction chamber (15); The first reaction chamber (15) is used to prepare water molecules from residual hydrogen molecules in the flue gas and oxygen molecules generated by the anode reaction chamber (143); The electrolytic cell (16) is used for electrolyzing water molecules to generate oxygen molecules and hydrogen molecules.

9. The natural gas hydrogen blended power plant hydrogen blended combustion and carbon capture system according to claim 7, characterized in that: The natural gas hydrogen blended power plant hydrogen blended combustion and carbon capture system further includes a first power generation unit and a second power generation unit; The first power generation unit comprises a solid-state battery (18), which is arranged at the outlet of the heat exchanger and is used to absorb heat from high-temperature flue gas to generate electricity; The second power generation unit comprises a second heat exchanger (19), a water source heat pump (20), a regeneration tower (21), a steam turbine (22) and a generator (23) connected in sequence; The second heat exchanger (19) comprises a shell, a first heat exchange tube, a second heat exchange tube and a circulation pump, wherein the circulation pump drives the heat exchange medium in the first heat exchange tube and the second heat exchange tube to circulate respectively, one end of each of the first heat exchange tube and the second heat exchange tube is arranged in the shell so that the first heat exchange tube and the second heat exchange tube exchange heat in the shell, the other end of the first heat exchange tube is surrounded by the outer wall of the carbon dioxide delivery pipeline, and the other end of the second heat exchange tube is surrounded by the outer wall of the water source heat pump (20); The water source heat pump (20) provides thermal energy for the regeneration tower (21), so that high-temperature and high-pressure steam is generated in the regeneration tower (21); the steam turbine (22) is connected to the steam outlet of the regeneration tower (21), receives steam power and outputs mechanical energy; the generator (23) is mechanically connected to the output shaft of the steam turbine (22), and converts the mechanical energy into electrical energy.

10. The natural gas hydrogen blended power plant hydrogen blended combustion and carbon capture system according to claim 7, characterized in that It also includes an intelligent control system, which includes a controller, a first electrically controlled valve (25) is provided on the first outlet (131), and a second electrically controlled valve (26) is provided on the second outlet (132); The controller is electrically connected to the first electrically controlled valve (25) and is used to control the opening of the first electrically controlled valve (25); The controller is electrically connected to the second electrically controlled valve (26) and is used to control the opening of the second electrically controlled valve (26).

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