Integrated apparatus for co2 capture coupled with synthetic fuel production from coal-fired power plants

Abstract

The utility model relates to flue gas separation technical field discloses a kind of integrated device of coal-fired power plant carbon dioxide capture coupling synthetic fuel preparation, and the integrated device of coal-fired power plant carbon dioxide capture coupling synthetic fuel preparation includes installation platform, carbon dioxide capture component and synthetic fuel preparation component, carbon dioxide capture component is located on installation platform, carbon dioxide capture component is communicated with the flue gas outlet of coal power plant, for capturing carbon dioxide in flue gas;Synthetic fuel preparation component includes first inlet and second inlet, first inlet is communicated with the carbon dioxide outlet of carbon dioxide capture component, second inlet is input hydrogen, and synthetic fuel preparation component is used to form liquefied hydrocarbon with hydrogen and carbon dioxide reaction.According to the integrated device of coal-fired power plant carbon dioxide capture coupling synthetic fuel preparation of the utility model, avoid the secondary compression, long-distance transportation and intermediate storage etc. link when carbon dioxide synthetic fuel, increase the utilization rate of carbon dioxide.

Description

Technical Field

[0001] This utility model relates to the field of flue gas separation technology, and in particular to an integrated device for carbon dioxide capture and coupled synthesis of fuels in coal-fired power plants. Background Technology

[0002] my country's coal-fired power capacity has long remained above 1 billion kilowatts, and coal-fired power units remain a crucial foundation for the stable operation of the power system. A typical 600MW coal-fired unit can emit over 10 billion Nm³ of flue gas annually, with a carbon dioxide volume fraction typically between 12% and 15%, resulting in annual carbon dioxide emissions exceeding 4 million tons per unit. With the advancement of energy conservation and emission reduction targets, the coal-fired power industry is facing unprecedented pressure to reduce emissions, making carbon dioxide capture and resource utilization an inevitable direction for the transformation and development of coal-fired power. Currently, the main approaches to carbon dioxide control in coal-fired power plants are capture and storage or low-value-added utilization, lacking a stable, high-value, and large-scale resource conversion system. On the one hand, the simple storage approach involves high investment and operating costs, placing a long-term burden on the economics of coal-fired power enterprises; on the other hand, existing carbon dioxide utilization is mostly concentrated in food-grade, chemical raw material-grade, or oil displacement fields, with limited capacity to absorb the massive carbon dioxide emissions from coal-fired power plants.

[0003] Meanwhile, synthetic fuels, as an important low-carbon alternative energy source in aviation, shipping, and high-end transportation, are considered one of the key directions for the resource utilization of carbon dioxide. However, existing synthetic fuel plants generally adopt an independent construction model, requiring additional carbon dioxide purification, compression, storage, transportation, and supply systems. This results in high engineering investment, low energy efficiency, and difficulty in achieving close integration with coal-fired power plants. Utility Model Content

[0004] This invention aims to solve at least one of the technical problems existing in the prior art. To this end, this invention proposes an integrated device for carbon dioxide capture and coupled synthesis of fuels in coal-fired power plants. This integrated device avoids the secondary compression, long-distance transportation, and intermediate storage required during carbon dioxide synthesis, thereby increasing the utilization rate of carbon dioxide.

[0005] An integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant, according to an embodiment of the present invention, includes: an installation platform; a carbon dioxide capture component disposed on the installation platform and connected to the flue gas outlet of the coal-fired power plant for capturing carbon dioxide in the flue gas; and a synthetic fuel preparation component disposed on the installation platform, the synthetic fuel preparation component including a first inlet and a second inlet, the first inlet being connected to the carbon dioxide outlet of the carbon dioxide capture component, the second inlet being through which hydrogen is introduced, and the synthetic fuel preparation component being used to react hydrogen with carbon dioxide to form liquefied hydrocarbons.

[0006] According to an embodiment of the present invention, an integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant is provided. By simultaneously setting up a carbon dioxide capture component and a synthetic fuel preparation component on the same installation platform, the synthetic fuel preparation component is used to react hydrogen with carbon dioxide to form liquefied hydrocarbons. Carbon dioxide extracted from the flue gas produced by the coal-fired power plant can be combined with hydrogen to produce synthetic liquefied hydrocarbons and other fuels, thus avoiding the secondary compression, long-distance transportation and intermediate storage of carbon dioxide, and increasing the utilization rate of carbon dioxide.

[0007] In some embodiments of this utility model, the carbon dioxide capture assembly includes: a flue gas pretreatment assembly, which is located downstream of the desulfurization and denitrification device of the coal-fired power plant, and includes an electrostatic precipitator, a wet desulfurization tower, and a wet electrostatic precipitator arranged sequentially; an adsorption tower, the flue gas inlet of which is connected to the outlet of the wet electrostatic precipitator, the adsorption tower containing an adsorbent liquid for adsorbing carbon dioxide, the adsorption tower having a first outlet and a second outlet, the first outlet being located at the upper end of the adsorption tower for discharging the flue gas after carbon dioxide removal, and the second outlet being located at the lower end of the adsorption tower; and a desorption tower, which has a third inlet and a third outlet, the third inlet being connected to the second outlet, the desorption tower for separating carbon dioxide from the adsorbent liquid, and the third outlet being connected to the first inlet for supplying carbon dioxide to the synthetic fuel preparation assembly.

[0008] In some embodiments of this utility model, the carbon dioxide capture assembly further includes a carbon dioxide compression assembly, which is connected to both the third outlet and the first inlet and is used to compress carbon dioxide.

[0009] In some embodiments of this utility model, the carbon dioxide capture assembly further includes a conveying assembly, wherein the adsorption tower is provided with a liquid inlet, the desorption tower is provided with a fourth outlet, and the conveying assembly is connected to both the liquid inlet and the fourth outlet, for guiding the adsorbed liquid after carbon dioxide separation in the desorption tower to the adsorption tower.

[0010] In some embodiments of this utility model, the synthetic fuel preparation assembly includes: a preheater, which is connected to both the first inlet and the second inlet, and is used to heat carbon dioxide and hydrogen entering the preheater; a reactor, whose inlet is connected to the outlet of the preheater, for hydrogenating carbon dioxide to form initial reactants; and a separation assembly, whose inlet is connected to the outlet of the reactor, for decomposing the initial reactants into solid reactants, liquefied hydrocarbons, and gaseous reactants.

[0011] In some embodiments of this utility model, the synthetic fuel preparation assembly further includes: a first compression assembly, which is connected to both the separation assembly and the preheater, and is used to transport the gaseous reactants separated by the separation assembly back to the preheater.

[0012] In some embodiments of this utility model, the synthetic fuel preparation assembly further includes: a phase change heat transfer loop structure, the phase change heat transfer loop structure including a phase change temperature controller, the phase change temperature controller being filled with a phase change material, the phase change temperature controller having heat-conducting fins inside, the heat-conducting fins extending along the axial direction of the phase change temperature controller, the phase change temperature controller having a first loop and a second loop, the first loop flowing through the outer wall of the reactor to absorb heat, and the second loop flowing through the preheater to preheat the carbon dioxide and hydrogen entering the preheater.

[0013] In some embodiments of this utility model, the synthetic fuel preparation assembly further includes: a pressure blending structure, the pressure blending structure being disposed upstream of the preheater, the pressure blending structure including a pressure sensor for detecting the pressure of carbon dioxide and hydrogen.

[0014] In some embodiments of this utility model, the integrated device for carbon dioxide capture and coupled synthesis fuel preparation in a coal-fired power plant further includes a hydrogen preparation device, which includes an electrolytic cell stack. The electrolytic cell stack is fed with raw water and KOH alkaline solution. The electrolytic cell stack prepares hydrogen and oxygen through electrolysis and delivers the hydrogen to the synthesis fuel preparation component.

[0015] In some embodiments of this utility model, the hydrogen production apparatus further includes a hydrogen compression assembly, which is connected to both the hydrogen outlet of the electrolyzer and the synthetic fuel production assembly, and is used to compress hydrogen.

[0016] Additional aspects and advantages of this invention will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. Attached Figure Description

[0017] The above and / or additional aspects and advantages of this utility model will become apparent and readily understood from the description of the embodiments taken in conjunction with the following drawings, in which:

[0018] Figure 1 This is a schematic diagram of an integrated device for carbon dioxide capture and coupled synthesis of fuels in a coal-fired power plant, according to an embodiment of the present invention.

[0019] Figure label:

[0020] 100. An integrated device for carbon dioxide capture coupled with synthetic fuel preparation in coal-fired power plants;

[0021] 1. Carbon dioxide capture assembly; 11. Flue gas pretreatment assembly; 111. Electrostatic precipitator; 112. Wet desulfurization tower; 113. Wet electrostatic precipitator; 12. Adsorption tower; 121. First outlet; 122. Second outlet; 13. Desorption tower; 131. Third inlet; 132. Third outlet; 14. Carbon dioxide compression assembly; 141. Carbon dioxide refrigerated dryer; 142. Carbon dioxide buffer tank; 143. Carbon dioxide compressor; 15. Conveying assembly; 151. Gas-liquid separator; 152. Rich solution circulation pump; 153. Heating heat exchanger; 154. Heating regenerator; 155. Cooling heat exchanger; 156. Make-up liquid mixer; 157. Lean solution circulation pump; 158. Water cooler; 159. Condenser; 16. Condensate pump;

[0022] 2. Synthetic fuel preparation components; 21. Preheater; 22. Reactor; 23. Separation components; 231. Wax separator; 232. Heavy separator; 233. Cold trap; 24. First compression assembly; 241. Fine filter; 242. Circulating compressor; 25. Phase change heat transfer loop structure; 251. Phase change temperature controller; 2511. First loop; 2512. Second loop; 252. Shielded pump; 26. Isobaric blending structure; 27. First inlet; 28. Second inlet;

[0023] 3. Hydrogen production apparatus; 31. Electrolyzer stack; 32. Hydrogen compression assembly; 33. Multi-media activated carbon filter; 34. Water softener; 35. Security filter; 36. Solution buffer tank; 371. Oxygen-side gas-liquid separator; 372. Oxygen-side refrigerated dryer; 373. Oxygen-side desiccant dryer; 374. Oxygen buffer tank; 381. Hydrogen-side gas-liquid separator; 382. Hydrogen-side refrigerated dryer; 383. Hydrogen-side desiccant dryer; 384. Hydrogen buffer tank. Detailed Implementation

[0024] The embodiments of this utility model are described in detail below. Examples of these embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain this utility model, and should not be construed as limiting this utility model.

[0025] In the description of this utility model, it should be understood that the terms "center," "longitudinal," "transverse," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential," etc., indicating the orientation or positional relationship shown in the accompanying drawings, are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model. Furthermore, features defined with "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this utility model, unless otherwise stated, "a plurality of" means two or more.

[0026] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0027] The following description, with reference to the accompanying drawings, describes an integrated apparatus 100 for the combined carbon dioxide capture and synthesis of fuels from a coal-fired power plant, according to an embodiment of the present invention.

[0028] like Figure 1 As shown, the integrated device 100 for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to an embodiment of the present invention includes an installation platform, a carbon dioxide capture component 1, and a synthetic fuel preparation component 2.

[0029] Specifically, the carbon dioxide capture component 1 is installed on the installation platform and is connected to the flue gas outlet of the coal-fired power plant. It is used to capture carbon dioxide in the flue gas, so that the clean flue gas after capturing carbon dioxide can meet the emission standards, making the emission of flue gas more environmentally friendly.

[0030] The synthetic fuel preparation component 2 is mounted on the installation platform. The synthetic fuel preparation component 2 includes a first inlet 27 and a second inlet 28. The first inlet 27 is connected to the carbon dioxide outlet of the carbon dioxide capture component 1, and the second inlet 28 is used to introduce hydrogen. The synthetic fuel preparation component 2 is used to react hydrogen and carbon dioxide to form liquefied hydrocarbons. The carbon dioxide extracted from the flue gas produced by the coal-fired power plant can be combined with hydrogen to produce synthetic liquefied hydrocarbons and other fuels, avoiding the secondary compression, long-distance transportation and intermediate storage of carbon dioxide, and increasing the utilization rate of carbon dioxide.

[0031] According to the embodiment of this utility model, the integrated device 100 for carbon dioxide capture and synthetic fuel preparation in a coal-fired power plant simultaneously sets up a carbon dioxide capture component 1 and a synthetic fuel preparation component 2 on the same installation platform. The synthetic fuel preparation component 2 is used to react hydrogen with carbon dioxide to form liquefied hydrocarbons. The carbon dioxide extracted from the flue gas produced by the coal-fired power plant can be combined with hydrogen to produce synthetic liquefied hydrocarbons and other fuels, avoiding the secondary compression, long-distance transportation and intermediate storage of carbon dioxide, and increasing the utilization rate of carbon dioxide.

[0032] In some embodiments of this utility model, such as Figure 1 As shown, the carbon dioxide capture assembly 1 includes a flue gas pretreatment assembly 11, an adsorption tower 12, and a desorption tower 13. The flue gas pretreatment assembly 11 is located downstream of the desulfurization and denitrification unit in a coal-fired power plant. The flue gas pretreatment assembly 11 includes an electrostatic precipitator 111, a wet desulfurization tower 112, and a wet electrostatic precipitator 113 arranged sequentially. The flue gas inlet of the adsorption tower 12 is connected to the outlet of the wet electrostatic precipitator 113. The adsorption tower 12 contains an adsorbent liquid for adsorbing carbon dioxide. The adsorption tower 12 has a first outlet 121 and a second outlet 122. The first outlet 121 is located at the upper end of the adsorption tower 12 and is used to discharge the flue gas after carbon dioxide removal. The second outlet 122 is located at the lower end of the adsorption tower 12. The adsorption temperature of the adsorption tower 12 can be 40℃~60℃.

[0033] Among them, the electrostatic precipitator 111 is used to remove large particulate fly ash from the flue gas, reducing the dust concentration from 10g / Nm³–30g / Nm³ to below 30mg / Nm³; the wet desulfurization tower 112 adopts the limestone-gypsum method for desulfurization, reducing the SO2 content to 10mg / Nm³–35mg / Nm³, while reducing the flue gas temperature to 45℃–55℃; the wet electrostatic precipitator 113 further removes acid mist and submicron particles, making the dust concentration of the flue gas entering the subsequent absorption system below 5mg / Nm³.

[0034] The adsorbent can be an amine absorbent. The treated flue gas enters the adsorption tower 12 from bottom to top and comes into full contact with the countercurrent sprayed amine absorbent. CO2 is absorbed to form a rich liquid. The purified flue gas is discharged through the first outlet 121 at the top of the tower, and the rich liquid flows out of the adsorption tower 12 through the second outlet 122.

[0035] The stripping tower 13 has a third inlet 131 and a third outlet 132. The third inlet 131 is connected to the second outlet 122. The stripping tower 13 is used to separate carbon dioxide from the adsorbent liquid. The third outlet 132 is connected to the first inlet 27 and is used to supply carbon dioxide to the synthetic fuel preparation component 2. At this time, carbon dioxide in the adsorbent liquid is precipitated. The adsorbent liquid can be reused after removing carbon dioxide, reducing the manufacturing cost of the carbon dioxide capture component 1. The operating pressure of the stripping tower 13 is 0.15 MPa to 0.25 MPa, and the stripping temperature is 110℃ to 130℃.

[0036] In some embodiments of this utility model, such as Figure 1 As shown, the carbon dioxide capture assembly 1 also includes a carbon dioxide compression assembly 14, which is connected to both the third outlet 132 and the first inlet 27, and is used to compress carbon dioxide. Specifically, the carbon dioxide compression assembly 14 includes a carbon dioxide refrigerated dryer 141, a carbon dioxide buffer tank 142, and a carbon dioxide compressor 143. The carbon dioxide obtained from the stripping tower 13 is deeply dehydrated by the carbon dioxide refrigerated dryer 141 to reduce the water content to below 0.5 vol%, and then enters the carbon dioxide buffer tank 142. The CO2 is pressurized by the carbon dioxide compressor 143 to a pressure level of 2 MPa-4 MPa, the same as that of hydrogen. The compressed carbon dioxide then enters the synthetic fuel preparation assembly 2 to facilitate better preparation of synthetic fuels.

[0037] In some embodiments of this utility model, such as Figure 1 As shown, the carbon dioxide capture assembly 1 also includes a conveying assembly 15. The adsorption tower 12 is provided with a liquid inlet, and the desorption tower 13 is provided with a fourth outlet. The conveying assembly 15 is connected to both the liquid inlet and the fourth outlet, and is used to guide the adsorbent liquid after carbon dioxide separation in the desorption tower 13 to the adsorption tower 12 to realize the reuse of the adsorbent liquid.

[0038] It is understood that a gas-liquid separator 151, a rich liquid circulation pump 152, and a heating heat exchanger 153 are provided between the third inlet 131 and the second outlet 122. The conveying assembly 15 includes a heating regenerator 154, a cooling heat exchanger 155, a makeup liquid mixer 156, a lean liquid circulation pump 157, and a water cooler 158. The carbon dioxide capture assembly 1 also includes a condenser 159. After the rich liquid at the bottom of the adsorption tower 12 enters the gas-liquid separator 151, the liquid is transported to the heating heat exchanger 153 via the rich liquid circulation pump 152. CO2 in the rich liquid is desorbed and released in the desorption tower 13. After being condensed by the condenser 159, the condensate is collected and recovered to the adsorption tower 12 by the condensate pump 16. The lean liquid after decomposition in the desorption tower 13 enters the heating regenerator 154 for temperature stabilization treatment, and then exchanges heat with the heating heat exchanger 153 at the top of the desorption tower 13 via the cooling heat exchanger 155. The heating heat exchanger can preheat the rich liquid that is about to enter the desorption tower 13. After the lean solution is analyzed, it is replenished with fresh solution by the replenishment mixer 156 and then transported by the lean solution circulation pump 157. After being cooled to 40℃–50℃ by the water cooler 158, it is returned to the adsorption tower 12 for recycling.

[0039] The carbon dioxide capture rate of the carbon dioxide capture component 1 is not less than 90%, preferably not less than 95%, and the volume fraction of the crude carbon dioxide gas obtained from the capture is not less than 95%. In addition, the carbon dioxide gas produced at the top of the stripping tower 13 is equipped with a carbon dioxide refrigerated dryer 141, and after condensation and dehydration, it enters the carbon dioxide compressor 143.

[0040] The carbon dioxide compression assembly 14 may also include a multi-stage centrifugal or reciprocating compressor, an interstage cooler, a condenser separator, and a dryer (molecular sieve or adsorption dryer) to compress carbon dioxide to the pressure level required for the reaction and to perform deep dehydration and impurity removal. The outlet pressure of the compressed carbon dioxide is 2MPa to 4MPa; the purity of the carbon dioxide is not less than 99%; the dew point of the water content is not higher than -40℃; and the oxygen content of the carbon dioxide gas compressed by the compressor after sealing improvement is not higher than 50ppm. The compressed and purified carbon dioxide enters the feed gas proportioning and mixing assembly through a check valve, a shut-off valve, and a pressure stabilizing buffer tank.

[0041] In some embodiments of this utility model, such as Figure 1 As shown, the synthetic fuel preparation component 2 includes a preheater 21, a reactor 22, and a separation component 23. The preheater 21 is connected to both the first inlet 27 and the second inlet 28. The preheater 21 is used to heat the carbon dioxide and hydrogen entering the preheater 21. The inlet of the reactor 22 is connected to the outlet of the preheater 21 and is used to hydrogenate the carbon dioxide to form the initial reactants. The inlet of the separation component 23 is connected to the outlet of the reactor 22 and is used to decompose the initial reactants into solid reactants, liquefied hydrocarbons, and gaseous reactants.

[0042] The preheater 21 can adopt a coaxial sleeve structure, with its shell side directly connected to the inlet gas of the reactor 22. This short-range thermal coupling structure eliminates the need for a traditional independent heating furnace located at the front end of the reactor 22, reducing system heat loss and shortening the length of the high-temperature logistics pipeline to reduce heat attenuation.

[0043] The separation assembly 23 includes a wax separator 231, a heavy liquid separator 232, and a cold trap 233. The product fluid from the reactor 22 outlet is transported to the wax separator 231, where gravity separation of the waxy product is first completed at 170°C, avoiding the need to cool all the product to a low temperature. The gaseous phase and light liquid phase after high-temperature separation enter the heavy liquid separator 232 and the cold trap 233 for further separation of the gas, liquefied hydrocarbons, and water phases. The liquefied hydrocarbon product is output as a synthetic fuel product, achieving purification of the liquefied hydrocarbons.

[0044] Reactor 22 is a multi-tube reactor, internally filled with a bifunctional composite catalyst. The design pressure of reactor 22 is not less than 5 MPa; the operating pressure is 2 MPa to 4 MPa; the operating temperature is 220℃ to 350℃; and the space velocity is 800 h⁻¹. - ¹~3000h - ¹. The reaction process includes the reverse water-gas shift reaction and the carbon chain growth reaction.

[0045] The separation assembly 23 includes at least one high-pressure gas-liquid separator 151, with a gas phase outlet and a liquid phase outlet. The gas phase outlet is connected to the tail gas recirculation assembly, and the liquid phase outlet is connected to the product refining assembly. The product refining assembly includes a stabilizing tower, a vacuum distillation tower, or a distillation tower group, used to separate the liquid phase product into: light fuel fraction, middle fraction, and heavy wax oil. The tail gas recirculation assembly includes a recirculation compressor 242, a recirculation ratio regulating valve, and an inert gas discharge branch. Unreacted hydrogen and carbon dioxide are returned to the preheater 21 after compression; inert gas enters the flare system through the discharge branch to ensure stable system operation. The recirculation ratio is 2 to 5 times, and the fresh gas replenishment ratio is not less than 20%.

[0046] In some embodiments of this utility model, such as Figure 1 As shown, the synthetic fuel preparation assembly 2 also includes a first compression assembly 24, which is connected to both the separation assembly 23 and the preheater 21. The first compression assembly 24 is used to return the gaseous reactants separated by the separation assembly 23 to the preheater 21. It is understood that the first compression assembly 24 includes a fine filter 241 and a recirculating compressor 242. The gaseous reactants are unreacted gases. These unreacted gases are returned to the preheater 21 via the fine filter 241 and the recirculating compressor 242 for preheating and then enter the reactor 22 for re-reaction, thereby improving the efficiency of the reactor 22 in producing liquefied hydrocarbons.

[0047] In addition, a low-load bypass circuit can be set at the inlet of the circulating compressor 242. When the system load is lower than 50% of the design load, the linear velocity and residence time in the reactor 22 can still be kept stable, avoiding the impact of frequent start-stop on the catalyst and equipment.

[0048] In some embodiments of this utility model, such as Figure 1 As shown, the synthetic fuel preparation assembly 2 also includes a phase change heat transfer loop structure 25, which includes a phase change temperature controller 251. The phase change temperature controller 251 is filled with a phase change material and has heat-conducting fins inside. The heat-conducting fins extend along the axial direction of the phase change temperature controller 251. The phase change temperature controller 251 has a first loop 2511 and a second loop 2512. The first loop 2511 flows through the outer wall of the reactor 22 to absorb heat, and the second loop 2512 flows through the preheater 21 to preheat the carbon dioxide and hydrogen entering the preheater 21.

[0049] Specifically, the phase change temperature controller 251 utilizes the exothermic reaction of the reactor 22 to preheat the feed temperature in the preheater 21 to 200℃–240℃. The preheated mixed gas enters the reactor 22 at a reaction pressure of 2MPa–4MPa and a reaction temperature of 300℃–380℃. The phase change heat transfer circuit structure 25 also includes a shielded pump 252, which guides the gas to the phase change temperature controller 251. The phase change temperature controller 251 is filled with a phase change material with a vaporization temperature of 250℃–350℃ and is equipped with axial heat-guiding fins to control the axial and radial temperature difference of the bed within the phase change temperature controller 251 within the range of ±10℃–15℃, thereby suppressing local hot spots within the phase change temperature controller 251 and extending the service life of the phase change material and catalyst.

[0050] The second loop 2512 forms the tube side of the preheater 21.

[0051] In some embodiments of this utility model, such as Figure 1 As shown, the synthetic fuel preparation assembly 2 also includes a pressure-matching blending structure 26, located upstream of the preheater 21. The pressure-matching blending structure 26 includes a pressure sensor for detecting the pressures of carbon dioxide and hydrogen. The pressure-matching blending structure 26 forms a matching transition zone, allowing mixing into the preheater 21 only when the pressure sensor detects a pressure difference between hydrogen and carbon dioxide of less than 0.2 MPa. Structurally, this avoids the need for additional mixing and compression equipment due to pressure mismatch, reducing compression energy consumption and equipment complexity.

[0052] The pressure blending structure 26 includes a static mixer, an online chromatographic analyzer, and a proportional control valve assembly to achieve precise metering and uniform mixing of carbon dioxide and hydrogen. Syngas is stably controlled, with CO2 and H2 volume fraction fluctuations not exceeding ±5%. The mixed gas is heated to 200℃~280℃ by the preheater 21 before entering the reactor 22.

[0053] In some embodiments of this utility model, such as Figure 1 As shown, the integrated device 100 for carbon dioxide capture and coupled synthesis fuel preparation in a coal-fired power plant also includes a hydrogen preparation device 3. The hydrogen preparation device 3 includes an electrolyzer stack 31, which is fed with raw water and KOH alkaline solution. The electrolyzer stack 31 prepares hydrogen and oxygen through electrolysis and delivers the hydrogen to the synthesis fuel preparation component 2.

[0054] Understandably, the raw water used for electrolysis is pretreated sequentially through a multi-media activated carbon filter 33, a water softener 34, and a security filter 35, and then mixed with KOH alkaline solution in a certain proportion to prepare a 20wt% KOH electrolyte. This electrolyte then enters the solution buffer tank 36 and is then stably transported to the electrolytic cell stack 31 by an alkaline solution pump. The electrolytic cell stack 31 operates at 0.3MPa–0.5MPa and 60℃–80℃, generating hydrogen and oxygen. After being dehydrated by the oxygen-side gas-liquid separator 371, the oxygen sequentially enters the oxygen-side refrigerated dryer 372 and the oxygen-side adsorption dryer 373 for deep dehydration. Subsequently, it is temperature-regulated by the oxygen-side cooler and transported to the oxygen buffer tank 374 by the oxygen-side circulating pump. The oxygen can be used as a by-product or fed into the boiler for combustion support.

[0055] After being dehydrated by the hydrogen-side gas-liquid separator 381, the hydrogen gas enters the hydrogen-side refrigerated dryer 382 and the hydrogen-side desiccant dryer 383 in sequence for deep dehydration, so that the water content is less than 0.5 vol%. Then, the hydrogen gas is cooled by the hydrogen-side cooler, and the treated hydrogen gas is sent to the hydrogen buffer tank 384 by the hydrogen-side circulation pump.

[0056] Among them, the electrolytic cell stack 31 can be an alkaline electrolytic cell stack.

[0057] In some embodiments of this utility model, such as Figure 1 As shown, the hydrogen production apparatus 3 also includes a hydrogen compression assembly 32, which is connected to both the hydrogen outlet of the electrolyzer stack 31 and the synthetic fuel production assembly 2, and is used to compress hydrogen. The hydrogen compression assembly 32 can compress hydrogen to 2-4 MPa, and the compressed hydrogen then enters the synthetic fuel production assembly 2 to facilitate better synthesis of synthetic fuels.

[0058] Preferably, the integrated device 100 for carbon dioxide capture and synthesis fuel preparation in a coal-fired power plant further includes a heat recovery component. The heat recovery component includes at least a flue gas waste heat exchanger and a reaction waste heat exchanger. Its output heat is supplied to the regeneration heat input interface of the carbon dioxide capture component 1 in the form of hot water or steam through a heat medium interface, so that the device realizes the heat coupling of the capture-conversion process.

[0059] Other components and operations of the integrated device 100 for carbon dioxide capture and coupled synthesis of fuels in a coal-fired power plant according to the embodiments of the present invention are known to those skilled in the art and will not be described in detail here.

[0060] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "illustrative embodiment," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the present invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples.

[0061] Although embodiments of the present invention have been shown and described, those skilled in the art will understand that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the present invention, the scope of which is defined by the claims and their equivalents.

Claims

1. An integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant, characterized in that, include: Installation platform; A carbon dioxide capture assembly is mounted on the installation platform and connected to the flue gas outlet of a coal-fired power plant for capturing carbon dioxide in the flue gas. A synthetic fuel preparation assembly is provided on the mounting platform. The synthetic fuel preparation assembly includes a first inlet and a second inlet. The first inlet is connected to the carbon dioxide outlet of the carbon dioxide capture assembly, and the second inlet is used to introduce hydrogen gas. The synthetic fuel preparation assembly is used to react hydrogen gas with carbon dioxide gas to form liquefied hydrocarbons.

2. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 1, characterized in that, The carbon dioxide capture assembly includes: A flue gas pretreatment assembly is located downstream of the desulfurization and denitrification unit of the coal-fired power plant. The flue gas pretreatment assembly includes an electrostatic precipitator, a wet desulfurization tower, and a wet electrostatic precipitator arranged in sequence. An adsorption tower is provided, wherein the flue gas inlet of the adsorption tower is connected to the outlet of the wet electrostatic precipitator, the adsorption tower contains an adsorption liquid for adsorbing carbon dioxide, and the adsorption tower has a first outlet and a second outlet. The first outlet is located at the upper end of the adsorption tower and is used to discharge the flue gas after carbon dioxide removal, and the second outlet is located at the lower end of the adsorption tower. The stripping column has a third inlet and a third outlet, the third inlet being connected to the second outlet, the stripping column being used to separate carbon dioxide from the adsorbent, and the third outlet being connected to the first inlet for supplying carbon dioxide to the synthetic fuel preparation assembly.

3. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 2, characterized in that, The carbon dioxide capture assembly also includes: A carbon dioxide compression assembly, which is connected to both the third outlet and the first inlet, is used to compress carbon dioxide.

4. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 2, characterized in that, The carbon dioxide capture assembly also includes: The conveying component is connected to both the liquid inlet and the fourth outlet of the adsorption tower, and is used to guide the adsorbed liquid after carbon dioxide separation in the desorption tower to the adsorption tower.

5. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 1, characterized in that, The synthetic fuel preparation components include: A preheater, which is connected to both the first inlet and the second inlet, is used to heat the carbon dioxide and hydrogen entering the preheater; A reactor, the inlet of which is connected to the outlet of the preheater, is used to perform hydrogenation of carbon dioxide to form initial reactants; A separation component, the inlet of which is connected to the outlet of the reactor, is used to decompose the initial reactants into solid reactants, liquefied hydrocarbons, and gaseous reactants.

6. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 5, characterized in that, The synthetic fuel preparation assembly also includes: A first compression component, which is connected to both the separation component and the preheater, is used to transport the gaseous reactants separated by the separation component back to the preheater.

7. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 5, characterized in that, The synthetic fuel preparation assembly also includes: A phase change heat transfer loop structure includes a phase change temperature controller, the phase change temperature controller is filled with a phase change material, and the phase change temperature controller has heat-conducting fins inside, the heat-conducting fins extending along the axial direction of the phase change temperature controller. The phase change temperature controller has a first loop and a second loop. The first loop flows through the outer wall of the reactor to absorb heat, and the second loop flows through the preheater to preheat the carbon dioxide and hydrogen entering the preheater.

8. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 5, characterized in that, The synthetic fuel preparation assembly also includes: A pressure-blending structure is provided upstream of the preheater, and the pressure-blending structure includes a pressure sensor for detecting the pressure of carbon dioxide and hydrogen.

9. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 1, characterized in that, Also includes: A hydrogen production apparatus, comprising an electrolytic cell stack, wherein raw water and KOH alkaline solution are introduced into the electrolytic cell stack, and the electrolytic cell stack produces hydrogen and oxygen through electrolysis and delivers the hydrogen to a synthetic fuel production assembly.

10. The integrated device for carbon dioxide capture coupled with synthetic fuel preparation in a coal-fired power plant according to claim 9, characterized in that, The hydrogen production apparatus further includes: A hydrogen compression assembly is connected to both the hydrogen outlet of the electrolyzer and the synthetic fuel preparation assembly, and is used to compress hydrogen.

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