A system for direct air carbon capture and conversion utilization coupling

Abstract

This invention discloses a system for coupling direct air carbon capture and conversion, comprising a direct air carbon capture unit, an electrolysis unit, a Fischer-Tropsch synthesis and upgrading unit, and a water-heat utilization unit connected in sequence. The water-heat utilization unit includes a heat exchanger and a water treatment unit. The Fischer-Tropsch synthesis and upgrading unit is connected to the water treatment unit via a third pipeline, the electrolysis unit is connected to the water treatment unit via fourth and sixth pipelines, and the direct air carbon capture unit is connected to the water treatment unit via a fifth pipeline. The Fischer-Tropsch synthesis and upgrading unit is connected to the heat exchanger via a first pipeline, and the direct air carbon capture unit is connected to the heat exchanger via a second pipeline. This invention seamlessly integrates the carbon capture and conversion processes, achieving full-chain optimization from CO2 removal to the generation of high-value-added products, meeting the heat cycle requirements of the equipment, improving heat utilization efficiency, and enabling wastewater recycling, thus reducing water consumption throughout the entire industrial chain.

Description

Technical Field

[0001] This utility model relates to the field of carbon dioxide capture and utilization technology, and in particular to a system for direct air carbon capture and conversion utilization coupling. Background Technology

[0002] Direct air carbon capture (DAC) is a technology that directly captures carbon dioxide from the atmosphere. The captured carbon dioxide can be utilized through various pathways, achieving net-negative carbon dioxide emissions. Carbon dioxide captured through DAC can be used for geological storage, achieving permanent isolation; it can also be converted into high-value-added products such as fuels, chemicals, and building materials. Converting carbon dioxide into fuel is the core pathway to achieving a closed-loop carbon cycle. By converting captured carbon dioxide into recyclable substances, dependence on fossil resources is reduced, and net emissions are lowered. The high demand and widespread application of synthetic fuels are crucial. Water resource technologies driven by renewable energy sources (such as wind and solar power) can combine CO2 with bound hydrogen in water through catalytic reactions to produce methanol, gasoline, diesel, or aviation fuel. For example, aviation fuel can be produced through the Fischer-Tropsch process, or zero-carbon gasoline can be developed. This closed-loop model integrates it into the energy and industrial system, achieving carbon recycling. While fuels offer the advantage of directly replacing traditional fossil fuels and are compatible with existing infrastructure, they face higher consumption and costs. In the future, with the decline in green hydrogen production costs and technological optimization, the economic viability and scalability potential of carbon dioxide conversion will be significantly enhanced, making it a key driver of carbon reduction goals.

[0003] Currently, the energy consumption of direct carbon dioxide capture (DAC) technology remains high, limiting its large-scale commercial application in terms of construction and use. DAC technology requires significant amounts of electricity and water resources to operate; if these resources come from non-renewable energy sources or water-scarce regions, it may have negative environmental impacts. Furthermore, the differences in market demand created by direct carbon dioxide capture technology and its applications due to differences in technology, models, and economic value create natural barriers, preventing the integration of capture and utilization and the recycling of resources. To address these issues, it is necessary to develop a device that can directly capture carbon dioxide from the air and convert it for utilization, achieving the transformation from carbon dioxide removal to utilization while also satisfying the requirements for the reuse of heat generated and water resources. Utility Model Content

[0004] In view of the shortcomings of the prior art described above, the purpose of this utility model is to provide a system for direct air carbon capture and conversion, which solves the problem in the prior art that carbon dioxide cannot be removed and utilized, and that heat and water resources cannot be reused.

[0005] This invention provides a system for directly capturing and converting carbon dioxide from the air, comprising a direct air carbon capture unit, an electrolysis unit, a Fischer-Tropsch synthesis and upgrading unit, and a water-thermal utilization unit connected in sequence.

[0006] The water-heat utilization unit includes a heat exchange device and a water treatment device. The Fischer-Tropsch synthesis and upgrading unit is connected to the water treatment device through a third pipeline. The electrolysis unit is connected to the water treatment device through a fourth and a sixth pipeline. The carbon dioxide capture unit is connected to the water treatment device through a fifth pipeline. The Fischer-Tropsch synthesis and upgrading unit is connected to the heat exchange device through a first pipeline. The direct air carbon capture unit is connected to the heat exchange device through a second pipeline.

[0007] In a preferred embodiment, the heat exchange device is selected from a heat exchanger, and the water treatment device is selected from a greywater reuse equipment.

[0008] Preferably, the direct air carbon capture unit is provided with an induced draft fan, a carbon dioxide capture device, a vacuum pump, a first cooler, and a carbon dioxide storage tank that are in sequential fluid communication along the gas inflow direction.

[0009] Preferably, the direct air carbon capture device is provided with a steam inlet and a steam outlet. The steam inlet is connected to a heat exchange device through a second pipeline, and the heat exchange device provides steam heat for desorbing carbon dioxide.

[0010] Preferably, the direct air carbon trap is further provided with a cooling water channel for introducing cooling water into the direct air carbon trap.

[0011] Preferably, the electrolysis unit includes a first compressor, an electrolyte storage tank, an electrolytic cell, an electrolysis post-processing module, and a gas storage tank, wherein the gas storage tank includes an oxygen storage tank and a carbon dioxide storage tank.

[0012] Preferably, the electrolytic cell includes an anode chamber, a cathode chamber, and an ion exchange membrane, wherein the ion exchange membrane is disposed between the anode chamber and the cathode chamber. Specifically, the anode catalyst used in the anode chamber is nickel foam, platinum mesh, or titanium mesh, and the cathode catalyst used in the cathode chamber is a nanocatalyst, a molecular catalyst, or a metal single-atom catalyst.

[0013] Preferably, both the anode and cathode chambers of the electrolytic cell are provided with inlets and outlets. The inlets of the anode and cathode chambers are connected to an electrolyte storage tank, which provides the electrolyte. Specifically, the electrolyte is one or more of sulfuric acid solution, potassium sulfate solution, potassium nitrate solution, and potassium hydroxide solution, preferably a sulfuric acid / potassium sulfate solution with a mass ratio of 5‰. The electrolyte is cooled by a second cooler before being introduced into the anode and cathode chambers of the electrolytic cell. Preferably, the inlet of the cathode chamber is connected to a compression device. Carbon dioxide flows from a carbon dioxide storage tank, is compressed by the compression device, and flows into the cathode chamber, where it undergoes a reduction reaction, simultaneously producing syngas. An oxidation reaction occurs on the surface of the anode chamber, producing oxygen.

[0014] Preferably, the electrolyte storage tank is connected to the outlet of the water treatment device of the water-heat utilization unit through a sixth pipeline, for reuse of the water recovered in the system, thereby reducing water waste.

[0015] Preferably, the electrolysis post-treatment module includes an anode electrolysis post-treatment module and a cathode electrolysis post-treatment module. The anode electrolysis post-treatment module is connected to the discharge port of the anode chamber of the electrolytic cell, and the cathode electrolysis post-treatment module is connected to the discharge port of the cathode chamber of the electrolytic cell. Furthermore, the cathode electrolysis post-treatment module includes a second gas-liquid separator and a fourth cooler connected in sequence. After the synthesis gas is separated into gas and liquid by the second gas-liquid separator, the gas is discharged from the gas outlet and enters the fourth cooler, while the liquid is discharged from the liquid outlet and fed into a water treatment device for recycling through a fourth pipeline.

[0016] Preferably, the gas storage tank includes an oxygen storage tank and a syngas storage tank. The oxygen storage tank is connected to the anode electrolysis post-treatment module, preferably to the outlet of the second gas-liquid separator 27, and is used to store the oxygen generated at the anode; the syngas storage tank is connected to the cathode electrolysis post-treatment module, preferably to the outlet of the first gas-liquid separator 24, and is used to store syngas.

[0017] In a preferred embodiment, the Fischer-Tropsch synthesis and upgrading unit is provided with a second compressor, a Fischer-Tropsch synthesizer, a Fischer-Tropsch post-processing module, and an upgrading module that are in sequential fluid communication along the gas inflow direction.

[0018] Preferably, the Fischer-Tropsch synthesizer further includes a first cooling water inlet and a first cooling water outlet. Fischer-Tropsch synthesis is an exothermic reaction. Cooling water is introduced through the first cooling water inlet to carry away a large amount of reaction heat and flows out through the first cooling water outlet. Preferably, the first cooling water outlet is connected to a heat exchange device through a first pipeline, which is used to absorb and carry away the heat released by the Fischer-Tropsch synthesis reaction when water turns into water vapor.

[0019] Preferably, the Fischer-Tropsch synthesis post-processing module includes a third gas-liquid separator and an oil-water separator. The third gas-liquid separator includes a gas outlet and a liquid outlet. The gas outlet is connected to a second compressor to reuse unreacted synthesis gas as circulating gas. The liquid outlet is connected to the oil-water separator.

[0020] Preferably, the oil-water separator further includes a product oil outlet and a water outlet to separate the product oil component and water in the liquid product. The oil outlet is also connected in sequence to a heating device and a pressurizing device to heat and pressurize the oil component, thereby upgrading the Fischer-Tropsch synthesis product.

[0021] Preferably, the upgrading unit includes a burner and a distillation column. The burner is connected to the gas outlet of the fourth gas-liquid separator to provide combustible gas for the burner, and the distillation column is connected to the upgraded oil outlet of the fourth gas-liquid separator.

[0022] This utility model has at least one of the following beneficial technical effects:

[0023] This invention develops an integrated and flexible industrial technology platform that seamlessly connects the carbon capture and conversion process, achieving full-chain optimization from CO2 removal to the generation of high-value-added products. It overcomes technological and market barriers, improves energy efficiency and economy, and compensates for the shortcomings of traditional industries operating in isolation and lacking collaboration. Through modular design and cross-domain compatibility, it promotes the deep integration of environmental protection and the chemical and energy industries; it meets the heat cycle requirements of the equipment, improving heat utilization; oxygen-enriched combustion accelerates the combustion reaction rate and reduces flue gas volume; and it enables wastewater recycling, reducing water consumption throughout the entire industrial chain. Attached Figure Description

[0024] Figure 1 This invention presents a system for direct air carbon capture and conversion.

[0025] Figure 2 The image shown is of the electrolytic cell in the electrolysis unit of this utility model.

[0026] Component designation explanation

[0027] 1 Direct air carbon capture unit 11 Exhaust fan 12 Direct air carbon capture device 121 Steam inlet 122 Steam outlet 13 vacuum pump 14 First Cooler 15 carbon dioxide storage tank 2 Electrolysis unit 21 Electrolyte storage tank 22 Second cooler 23 Electrolytic cell 231 Anode chamber 232 Cathode chamber 233 Anode chamber feed inlet 234 Cathode chamber feed inlet 235 Anode chamber outlet 236 Cathode chamber outlet 24 First gas-liquid separator 25 Third Cooler 26 Syngas storage tank 27 Second gas-liquid separator 28 Fourth cooler 29 Oxygen storage tank 210 First compressor 3 Fischer-Tropsch Synthesis and Upgrading Unit 31 Second compressor 32 Fifth cooler 33 Fischer-Tropsch synthesizer 331 First cooling hot water inlet 332 First cooling steam outlet 34 Third gas-liquid separator 341 Second cooling water inlet 342 Second cooling water outlet 35 Oil-water separator 36 heater 37 High pressure pump 38 Quality Improvement Module 381 Hydrocracking and Isomerization Reactors 382 Fourth gas-liquid separator 383 burner 3831 Third cooling water inlet 3832 Fourth cooling water inlet 384 Fifth gas-liquid separator 385 Distillation column 386 Seventh Cooler 387 Eighth Cooler 388 Sixth Cooler 4 Heat exchange and water treatment unit 41 heat exchanger 42 greywater treatment equipment 100 First pipeline 200 Second pipeline 300 Third pipeline 400 Fourth pipeline 500 Fifth pipeline 600 Sixth pipeline Detailed Implementation

[0028] The following specific examples illustrate the implementation of this utility model. Those skilled in the art can easily understand other advantages and functions of this utility model from the content disclosed in this specification.

[0029] Please see Figure 1-2It should be understood that the structures, proportions, sizes, etc., illustrated in the accompanying drawings are merely for illustrative purposes to aid those skilled in the art and are not intended to limit the scope of this invention. Therefore, they have no substantial technical significance. Any modifications to the structure, changes in proportions, or adjustments to size, without affecting the effectiveness and purpose of this invention, should still fall within the scope of the disclosed technical content. Furthermore, the terms "upper," "lower," "left," "right," "middle," and "one" used in this specification are merely for clarity and not intended to limit the scope of this invention. Changes or adjustments to their relative relationships, without substantially altering the technical content, should also be considered within the scope of this invention.

[0030] like Figure 1 As shown, a system for direct air carbon capture and conversion is coupled, comprising a direct air carbon capture unit 1, an electrolysis unit 2, a Fischer-Tropsch synthesis and upgrading unit 3, and a water-thermal utilization unit 4 connected in sequence.

[0031] The water-heat utilization unit 4 includes a heat exchange device 41 and a water treatment device 42. The Fischer-Tropsch synthesis and upgrading unit 1 is connected to the water treatment device 42 through a third pipeline 300. The electrolysis unit 2 is connected to the water treatment device 42 through a fourth pipeline 400 and a sixth pipeline 600. The direct air carbon capture unit 1 is connected to the water treatment device 42 through a fifth pipeline 500. The Fischer-Tropsch synthesis and upgrading unit 3 is connected to the heat exchange device 41 through a first pipeline 100. The direct air carbon capture unit 1 is connected to the heat exchange device 41 through a second pipeline 200.

[0032] Furthermore, the aforementioned heat exchange device recovers and reuses the heat generated by the system, meeting both cooling and heating requirements. The aforementioned water treatment device recycles and reuses the wastewater generated by the system, making full use of water resources and reducing waste.

[0033] In a preferred embodiment, the heat exchange device is selected from a heat exchanger, and the water treatment device is selected from a greywater reuse equipment.

[0034] In a preferred embodiment, the direct air carbon capture unit is provided with an induced draft fan 11, a direct air carbon capture device 12, a vacuum pump 13, a first condenser tower 14, and a carbon dioxide storage tank 15 that are sequentially fluidly connected along the gas inflow direction.

[0035] In this embodiment of the invention, air is directly drawn in by the exhaust fan 11 to obtain air containing carbon dioxide. Specifically, the exhaust fan 11 is connected to the input end of the direct air carbon trap 12.

[0036] Preferably, the direct air carbon trap 12 uses a solid adsorbent, liquid absorption, hygroscopic adsorption, or electrochemical solution to trap carbon dioxide in the air. Preferably, the direct air carbon trap 12 uses a solid adsorbent, preferably a resin-based carbon dioxide adsorbent. More preferably, the active functional group of the aforementioned solid adsorbent is one or both of amine groups and quaternary ammonium groups, preferably amine groups. Introducing amine groups into resin-based carbon dioxide adsorbents through chemical modification can significantly enhance the resin's adsorption capacity for carbon dioxide, accelerate the trapping rate, save trapping time, and improve trapping efficiency.

[0037] During adsorption, a large amount of air enters the direct air carbon trap 12. The weakly basic groups on the surface of the solid amine come into full contact with the carbon dioxide in the air and undergo a chemical reaction, thereby fixing a large amount of carbon dioxide on the surface of the solid amine adsorbent until saturation. When adsorption is saturated, high-concentration carbon dioxide is released by heating, thus completing a complete adsorption-desorption cycle. In a further embodiment, the adsorbent after desorbing carbon dioxide can be reused.

[0038] In a preferred embodiment, the direct air carbon capture device 12 is further provided with a steam inlet 121 and a steam outlet 122. The steam inlet 121 is connected to the outlet of the heat exchange device 41 through a second pipeline 200. The heat exchange device 41 provides the steam heat required for desorbing carbon dioxide for the purpose of desorbing carbon dioxide.

[0039] In a preferred embodiment, the direct air carbon capture device 12 is further provided with a cooling water passage for introducing cooling water into the carbon dioxide capture device to pre-cool the desorbed carbon dioxide.

[0040] In one specific embodiment, the aforementioned vacuum pump 13 is used to expel air from the carbon dioxide gas, preventing it from mixing into the carbon dioxide and causing a decrease in carbon dioxide concentration, and preventing the oxygen in the air from aging the adsorbent material under high temperature and high humidity conditions; the aforementioned first cooler 14 is used to cool the high-temperature carbon dioxide. Preferably, the aforementioned first cooler 14 is connected to the inlet of the water treatment device 42 through the fifth pipeline 500, and is used to recover cooling water.

[0041] In the above system, such as Figure 1 As shown, the electrolysis unit 2 is provided with a first compressor 210, an electrolysis cell 23, an electrolysis post-processing module, and a gas storage tank that are connected in sequence along the gas inflow direction. The gas storage tank includes an oxygen storage tank 29 and a syngas storage tank 26.

[0042] In a preferred embodiment, the main function of the electrolysis unit 2 is to reduce the high-purity carbon dioxide obtained from the direct air carbon capture unit 1 to carbon monoxide by electrochemical means. At the same time, the process of electrolyzing water will also produce hydrogen and oxygen. Different specifications of syngas can be obtained by adjusting the ratio of carbon monoxide and hydrogen.

[0043] In some embodiments of the present invention, the high-purity carbon dioxide gas obtained by the direct air carbon capture unit 1 is compressed by the first compressor 210 and then enters the electrolytic cell for electrolysis reaction.

[0044] Specifically, such as Figure 2 As shown, the electrolytic cell 23 includes an anode chamber 231 and a cathode chamber 232. Specifically, the anode catalyst used in the anode chamber 231 is nickel foam, platinum mesh, or titanium mesh, and the cathode catalyst used in the cathode chamber 232 is a nanocatalyst, a molecular catalyst, or a metal single-atom catalyst.

[0045] In one specific embodiment, both the anode chamber 231 and the cathode chamber 232 of the electrolytic cell are provided with inlets and outlets. The inlets 233 and 234 of the anode chamber 231 and the cathode chamber 232 are connected to an electrolyte storage tank 21. The outlet of the electrolyte storage tank 21 is connected to the inlets 233 and 234 of the anode chamber and the cathode chamber, respectively. The electrolyte storage tank 21 is used to provide electrolyte. Specifically, the electrolyte is one or more of sulfuric acid solution, potassium sulfate solution, potassium nitrate solution, and potassium hydroxide solution, preferably a sulfuric acid / potassium sulfate solution with a mass ratio of 5‰. The electrolyte is cooled by the second cooler 22 and then introduced into the anode chamber 231 and the cathode chamber 232 of the electrolytic cell. Furthermore, the feed inlet 234 of the cathode chamber of the electrolytic cell is connected to the output end of the first compressor 210. Carbon dioxide flows from the carbon dioxide storage tank 15 into the cathode chamber 232 of the electrolytic cell after being compressed by the first compressor 210. Subsequently, a reduction reaction occurs in the cathode chamber 232, generating syngas. An oxidation reaction occurs on the surface of the anode chamber 231 of the electrolytic cell, producing oxygen.

[0046] Further preferred, such as Figure 1 As shown, the inlet of the electrolyte storage tank 21 is connected to the outlet of the water treatment device 42 of the water-heat utilization unit 4 through the sixth pipeline 600, so as to reuse the water recovered in the system and reduce water waste.

[0047] In a further embodiment, the above-mentioned electrolysis post-treatment module includes an anode electrolysis post-treatment module and a cathode electrolysis post-treatment module. The anode electrolysis post-treatment module is connected to the discharge port 235 of the anode chamber of the electrolytic cell, and the cathode electrolysis post-treatment module is connected to the discharge port 236 of the cathode chamber of the electrolytic cell. Further, the above-mentioned anode electrolysis post-treatment module includes a first gas-liquid separator 24 and a third cooler 25 connected in sequence. After the synthesis gas is separated into gas and liquid by the first gas-liquid separator 24, the gas is discharged from the gas outlet and enters the third cooler 25, while the liquid is discharged from the liquid outlet and flows through a fourth pipeline 400 into a water treatment device 42 for recycling. Still further, the above-mentioned cathode electrolysis post-treatment module includes a second gas-liquid separator 27 and a fourth cooler 28 connected in sequence. After the synthesis gas is separated into gas and liquid by the second gas-liquid separator 27, the gas is discharged from the gas outlet and enters the fourth cooler 28, while the liquid is discharged from the liquid outlet and flows through a fourth pipeline 400 into a water treatment device 42 for recycling.

[0048] In a further embodiment, the gas storage tank includes an oxygen storage tank 29 and a syngas storage tank 26. Preferably, the oxygen storage tank 29 is connected to the anode electrolysis post-processing module, and more preferably to the outlet of the second gas-liquid separator 27, for storing oxygen generated at the anode; the syngas storage tank 26 is connected to the cathode electrolysis post-processing module, and more preferably to the outlet of the first gas-liquid separator 24, for storing syngas.

[0049] In the above system, such as Figure 1 As shown, the Fischer-Tropsch synthesis and upgrading unit is provided with a second compressor 31, a Fischer-Tropsch synthesizer 33, a Fischer-Tropsch synthesis post-processing module, and an upgrading module 38 that are in sequential fluid communication along the gas inflow direction.

[0050] In the above system, the output end of the syngas storage tank 26 is connected to the second compressor 31, which is used to compress the syngas to the pressure required for Fischer-Tropsch synthesis before it is fed into the Fischer-Tropsch synthesizer 33. The syngas flowing into the second compressor 33 is first compressed to the pressure required for Fischer-Tropsch synthesis before being fed into the Fischer-Tropsch synthesizer 33. Preferably, the above-mentioned Fischer-Tropsch synthesis and upgrading unit also includes a fifth cooler 32, which is located between the second compressor 33 and the Fischer-Tropsch synthesizer 33. The compressed syngas is cooled by protective cooling water in the fifth cooler 32 before being fed into the Fischer-Tropsch synthesizer 33 for reaction.

[0051] In a preferred embodiment, the Fischer-Tropsch synthesizer 33 further includes a first cooling hot water inlet 331 and a first cooling steam outlet 332. Fischer-Tropsch synthesis is an exothermic reaction; cooling hot water is introduced through the first cooling hot water inlet 331 to carry away a large amount of reaction heat and flows out through the first cooling steam outlet 332. Preferably, the first cooling steam outlet 332 is connected to the inlet of the heat exchange device 41 via a first pipe 100, used to absorb and carry away the heat released by the Fischer-Tropsch synthesis reaction as water is converted into steam. Excess steam from the Fischer-Tropsch synthesizer 33 is preferably used to heat other equipment units, eliminating the need for external steam input.

[0052] In a preferred embodiment, the Fischer-Tropsch synthesis post-processing module includes a third gas-liquid separator 34 and an oil-water separator 35. The third gas-liquid separator 34 includes a gas outlet and a liquid outlet. The gas outlet is connected to a second compressor 31 to reuse unreacted synthesis gas as circulating gas; the liquid outlet is connected to the oil-water separator 35. Preferably, the third gas-liquid separator 34 further includes a second cooling water inlet 341 and a second cooling water outlet 342 to further cool the crude Fischer-Tropsch synthesis product. The second cooling water outlet 342 is connected to the inlet of the heat exchange device 41 via a first pipeline 100 for recovering and reusing the heat from the crude Fischer-Tropsch synthesis product.

[0053] In a preferred embodiment, the oil-water separator 35 further includes an oil outlet and a water outlet to separate the oil component and water in the Fischer-Tropsch crude synthesis product.

[0054] In a preferred embodiment, the heater 36 and high-pressure pump 37 are connected between the oil-water separator 35 and the upgrading module 38. The heater 36 and high-pressure pump 37 heat and pressurize the oil components, providing a high-temperature and high-pressure environment for the Fischer-Tropsch synthesis crude oil, ensuring the smooth progress of the subsequent hydrocracking and isomerization reactions. Furthermore, the water outlet of the oil-water separator is connected to the inlet of the water treatment device 42 via a third pipeline 300 for the recovery and reuse of water components.

[0055] In one specific embodiment, the upgrading module 38 includes a hydrocracking and isomerization reactor 381 and a fourth gas-liquid separator 382 connected in sequence. The upgrading unit 38 refines Fischer-Tropsch synthesis products into synthetic fuels, particularly aviation turbine fuels, diesel, paraffin oil, and / or crude gas oils, such as kerosene (SAF - Sustainable Aviation Fuel), crude gasoline, or light gasoline. To manufacture industrial-grade kerosene, diesel, and crude gasoline, hydroisomerization and hydrocracking are used to convert the paraffin products from Fischer-Tropsch synthesis into isomerized oil-gas mixtures to produce high-value aviation turbine fuels with cooling properties.

[0056] More preferably, the hydrocracking and isomerization reactor 381 further includes a hydrogen inlet to provide the hydrogen required for the hydroisomerization and hydrogenation cracking reactions. Furthermore, the hydrogen is provided by the electrolyzer of the electrolysis module, or by an external hydrogen tanker truck or hydrogen cylinder.

[0057] More specifically, a sixth cooler 388 is connected between the aforementioned hydrocracking and isomerization reactor 381 and the fourth gas-liquid separator 382. The isomerized oil-gas mixture from the Fischer-Tropsch synthesis crude oil, after being cooled by the sixth cooler 388, enters the fourth gas-liquid separator 382 to separate the combustible gas and the upgraded oil.

[0058] In one specific embodiment, the above-mentioned upgrading module further includes a burner 383 and a distillation column 385. The burner 383 is connected to the gas outlet of the fourth gas-liquid separator 382 to provide combustible gas for the burner 383, and the distillation column 385 is connected to the upgraded oil outlet of the fourth gas-liquid separator 382. Preferably, the burner 383 further includes an oxygen inlet connected to an oxygen storage tank 29 for oxygen-enriched combustion of combustible gas and oxygen. The burner 383 also includes a third cooling water inlet 3831 and a third cooling water outlet 3832. The third cooling water outlet 3832 is connected to the inlet of the heat exchange device 41 through a first pipeline 100 and serves as a heat source for the direct air carbon capture unit 1.

[0059] Specifically, the outlet of the burner 383 is also connected to a fifth gas-liquid separator 384, which includes a gas outlet and a liquid outlet. The gas outlet is connected to the inlet of the heat exchange device 41 through the first pipeline 100 to provide heat to the carbon dioxide capture module 1. The liquid outlet is connected to the inlet of the water treatment device 42 through the third pipeline 300 to provide electrolyte to the electrolyte storage tank 21.

[0060] Preferably, the distillation column includes a top condenser and a bottom reboiler. Through distillation, the upgraded oil product is separated based on the differences in volatility of its components, causing the lighter components (low-boiling-point components) to concentrate at the top of the column and the heavier components (high-boiling-point components) to concentrate at the bottom, thus achieving separation. The distillation column includes 8-12 theoretical plates, breaking down the upgraded oil product into different distillates. After cooling in the seventh cooler 386 and the eighth cooler 387, products are obtained, such as turbo fuel and diesel, aviation turbo fuel and crude gas oil, aviation turbo fuel, crude gasoline and diesel, or similar heavy oil products.

[0061] In a preferred embodiment, the cooling water outlets of the seventh cooler 386 and the eighth cooler 387 are connected to the inlet of the heat exchange device to further provide heat for the desorption of carbon dioxide.

[0062] This invention couples carbon capture and conversion, achieving full-chain optimization from CO2 removal to the generation of high-value-added products. It breaks through technological and market barriers, improves energy efficiency and economy, and compensates for the shortcomings of traditional industries operating independently and lacking collaboration. By using oxygen-enriched combustion of combustible gases from hydrocracking and isomerization, it fully utilizes the product gas and recovers and utilizes the heat generated by Fischer-Tropsch synthesis, hydrocracking and isomerization reactions, and oxygen-enriched combustion in the Fischer-Tropsch synthesis and upgrading units. This allows the heat requirements for carbon dioxide desorption to be met without external heat. Wastewater from each unit of the system can be recycled, reducing the water consumption of the entire industrial chain.

[0063] The above embodiments are merely illustrative of the principles and effects of this utility model and are not intended to limit the scope of this utility model. Any person skilled in the art can modify or alter the above embodiments without departing from the spirit and scope of this utility model. Therefore, all equivalent modifications or alterations made by those skilled in the art without departing from the spirit and technical concept disclosed in this utility model should still be covered by the claims of this utility model.

Claims

1. A system for direct air carbon capture and conversion coupled together, characterized in that, It includes a direct air carbon capture unit (1), an electrolysis unit (2), a Fischer-Tropsch synthesis and upgrading unit (3), and a water-heat utilization unit (4) connected in sequence. The water-heat utilization unit (4) includes a heat exchange device (41) and a water treatment device (42). The Fischer-Tropsch synthesis and upgrading unit (3) is connected to the water treatment device (42) through a third pipeline (300). The electrolysis unit (2) is connected to the water treatment device (42) through a fourth pipeline (400) and a sixth pipeline (600). The direct air carbon capture unit (1) is connected to the water treatment device (42) through a fifth pipeline (500). The Fischer-Tropsch synthesis and upgrading unit (3) is connected to the heat exchange device (41) through a first pipeline (100). The direct air carbon capture unit (1) is connected to the heat exchange device (41) through a second pipeline (200).

2. The system as described in claim 1, characterized in that, The direct air carbon capture unit is provided with a draft fan (11), a direct air carbon capture device (12), a vacuum pump (13), a first condenser tower (14), and a carbon dioxide storage tank (15) that are connected in sequence along the gas inflow direction. The electrolysis unit (2) is provided with a first compressor (210), an electrolysis cell (23), an electrolysis post-processing module, and a gas storage tank connected in sequence along the gas inflow direction. The gas storage tank includes an oxygen storage tank (29) and a syngas storage tank (26). The Fischer-Tropsch synthesis and upgrading unit is provided with a second compressor (31), a Fischer-Tropsch synthesizer (33), a Fischer-Tropsch synthesis post-processing module, and an upgrading module (38) that are sequentially fluidly connected along the gas inflow direction.

3. The system as described in claim 2, characterized in that, The direct air carbon trap (12) is provided with a steam inlet (121) and a steam outlet (122), and the steam inlet (121) is connected to the outlet of the heat exchange device (41) through a second pipeline (200).

4. The system as described in claim 2, characterized in that, The electrolytic cell (23) includes an anode chamber (231) and a cathode chamber (232). The anode chamber (231) of the electrolytic cell (23) includes an anode chamber inlet (233) and an anode chamber outlet (235). The cathode chamber (232) of the electrolytic cell (23) includes a cathode chamber inlet (234) and a cathode chamber outlet (236). The outlet of the first compressor (210) is connected to the cathode chamber inlet (234) of the electrolytic cell.

5. The system as described in claim 4, characterized in that, The electrolysis unit also includes an electrolyte storage tank (21), the output port of which is connected to the anode chamber inlet (233) and the cathode chamber inlet (234), and the input port of which is connected to the outlet of the water treatment device (42) through a sixth pipeline; And / or, the electrolysis post-treatment module includes an anode electrolysis post-treatment module and a cathode electrolysis post-treatment module, the anode electrolysis post-treatment module being connected to the anode chamber outlet (235), and the cathode electrolysis post-treatment module being connected to the cathode chamber outlet (236).

6. The system as described in claim 5, characterized in that, The inlet of the oxygen storage tank is connected to the anode electrolysis post-treatment module, and the inlet of the syngas storage tank (26) is connected to the cathode electrolysis post-treatment module. And / or, the anodic electrolysis post-treatment module includes a first gas-liquid separator (24) and a third cooler (25) connected in sequence, and the liquid outlet of the first gas-liquid separator (24) is connected to a water treatment device (42) through a fourth pipeline (400). And / or, the cathode electrolysis post-treatment module includes a second gas-liquid separator (27) and a fourth cooler (28) connected in sequence, the second gas-liquid separator (27) being connected to the inlet of the water treatment device (42) via a fourth pipeline (400).

7. The system as described in claim 2, characterized in that, The Fischer-Tropsch synthesizer (33) further includes a first cooling hot water inlet (331) and a first cooling steam outlet (332), the first cooling steam outlet (332) being connected to the inlet of the heat exchange device (41) via a first pipeline (100); And / or, the Fischer-Tropsch synthesis post-processing module includes a third gas-liquid separator (34), an oil-water separator (35), a heater (36), and a high-pressure pump (37). The third gas-liquid separator (34) includes a gas outlet and a liquid outlet. The gas outlet is connected to a second compressor (31), and the liquid outlet is connected to the oil-water separator (35). The oil-water separator (35) includes an oil outlet and a water outlet. The oil outlet is connected in sequence to the heater (36) and the high-pressure pump (37). The water outlet is connected to the inlet of the water treatment device (42) through a third pipeline (300). And / or, the upgrading module (38) includes a hydrocracking and isomerization reactor (381) and a fourth gas-liquid separator (382) connected in sequence.

8. The system as described in claim 7, characterized in that, The hydrocracking and isomerization reactor (381) is provided with a hydrogen inlet for supplying hydrogen to the hydrocracking and isomerization reaction; And / or, the upgrading module further includes a burner (383) and a distillation column (385), the burner (383) being connected to the gas outlet of the fourth gas-liquid separator (382), and the distillation column being connected to the upgraded oil outlet of the fourth gas-liquid separator (382).

9. The system as described in claim 8, characterized in that, The burner (383) also includes an oxygen inlet, which is connected to the outlet of the oxygen storage tank (29); And / or, the burner (383) further includes a third cooling water inlet (3831) and a third cooling water outlet (3832), the third cooling water outlet (3832) being connected to the inlet of the heat exchange device (41) via a first pipe (100); And / or, the outlet of the burner (383) is also connected to a fifth gas-liquid separator (384), which includes a gas outlet and a liquid outlet. The gas outlet is connected to the inlet of the heat exchange device (41) through a first pipeline (100), and the liquid outlet is connected to the inlet of the water treatment device (42) through a third pipeline (300).

10. The system as described in claim 8, characterized in that, The distillation column includes a top condenser and a bottom reboiler. The top condenser enriches fuel oil products, and the bottom reboiler enriches heavy oil products.

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