Two-stage rotating wheel adsorption device and method for capturing carbon dioxide in flue gas

Abstract

The invention relates to the technical field of carbon dioxide trapping, in particular to a two-stage rotating wheel adsorption device and method for trapping carbon dioxide in flue gas, the two-stage rotating wheel adsorption device comprises a spray tower, a refrigerating unit, a dehumidification rotating wheel, a carbon trapping rotating wheel, a multi-stage compressor, a refrigerating and liquefying device, a CO2 storage tank and a flue gas fan, the implementation process of the carbon capture device comprises the steps that flue gas is introduced by a flue gas fan, firstly, the flue gas is cooled and dehumidified through a spray tower and a cooler, then the flue gas is dehumidified through a dehumidification rotating wheel, carbon capture is conducted through a carbon capture rotating wheel, and finally high-purity CO2 liquid is conveyed into a CO2 storage tank through a compressor and a refrigeration liquefaction device. The device has the characteristics of low desorption energy consumption, low gas circulation piezoresistance, continuous process and high heat recovery rate, the concentration of enriched CO2 is increased, the concentration of CO2 in flue gas after the carbon capture runner is relatively low, and the unit CO2 capture energy consumption can be greatly reduced while the CO2 removal rate and the enrichment concentration are ensured.

Description

Technical Field

[0001] The present invention relates to the technical field of carbon dioxide capture, and is a two-stage rotary adsorption device and method for capturing carbon dioxide (CO2) in flue gas. Background Art

[0002] It is of great significance to capture carbon dioxide from flue gas after combustion. Solvent absorption, as the most mature carbon dioxide capture technology, has been widely used. So far, from laboratory and pilot plant tests to large-scale plants worldwide, after a series of process optimization, the carbon capture energy consumption of this technology is between 1.8GJ / t CO2 and 2.5GJ / t CO2. However, there is still controversy about the economics of the total cost of more than 270 yuan / t CO2 generated by energy consumption and other maintenance, such as solution degradation loss and equipment corrosion protection. As another major carbon dioxide capture technology, traditional fixed bed adsorption technology has the advantages of ruggedness, low maintenance and no corrosion problems, but the carbon capture energy consumption is relatively high, which is 1.9GJ / t to 3.5GJ / t CO2. Although the technical feasibility of these two technologies has been verified, the long-term pursuit of reducing carbon capture energy consumption and reducing carbon footprint has never stopped.

[0003] As key technical factors, the structure of the adsorbent, the adsorption bed and the device should be well combined with the appropriate cyclic adsorption process to achieve the intensification of the carbon capture process. The traditional fixed bed structure is the simplest and is suitable for filling granular adsorbents, but it has problems such as large heat and mass transfer resistance, low bed utilization, unsatisfactory pressure drop, and large heat loss during temperature changes. In order to strengthen the carbon capture process based on adsorption, it is necessary to fully consider the impact of the adsorbent in the adsorption bed on gas flow, heat management and carbon dioxide enrichment.

[0004] At present, flue gas has the characteristics of low concentration and large flow, which makes the traditional chemical absorption liquid or adsorbent fixed bed face the problems of equipment corrosion and high pressure drop in practical application, resulting in large material consumption and high energy consumption. In addition, since the absorption or adsorption process is usually a non-continuous operation mode, it will also cause internal heat waste. Although a lot of research has been done on flue gas CO2 capture technology at home and abroad, the problem of high energy consumption has not been effectively solved.

[0005] The Chinese patent document with the publication number CN113975937A discloses a rotary adsorption capture device for CO2 in flue gas, including a rotor and a shell, wherein the shell is coated on the outside of the rotor, and the inside of the shell is provided with an adsorption zone, a desorption zone and a cooling zone, and the desorption zone is also connected to a self-circulating thermal desorption device for recovering the enriched gas, and the self-circulating thermal desorption device includes a heat exchanger and a circulation pipeline design, and the heat exchanger is connected to a waste heat pipeline for absorbing waste heat. However, in this technology, on the one hand, the flue gas passing through the adsorption zone of the rotor is directly discharged to the chimney, but this part of the gas is dry, pure, and has a high temperature, which is very suitable for preheating the gas in the desorption zone, and purging and cooling the cooling zone of the rotor, and it is not reasonably used; on the other hand, there is no spray tower for the front-end treatment of the flue gas, which will cause the flue gas temperature to be high and cannot meet the requirements of the rotor carbon capture material. At the same time, the desorption temperature required when the CO2 purity reaches more than 90% is relatively high.

[0006] In view of this, it is necessary to study a two-stage rotary adsorption device and method for capturing CO2 in flue gas to solve the above problems. Summary of the invention

[0007] The present invention provides a two-stage rotary adsorption device and method for capturing carbon dioxide in flue gas, which overcomes the shortcomings of the above-mentioned prior art and can effectively solve the problems of excessively high energy consumption of conventional carbon capture and low concentration of enriched CO2 in the process.

[0008] One of the technical solutions of the present invention is achieved through the following measures: a two-stage rotor adsorption device for capturing carbon dioxide in flue gas, comprising a spray tower, a refrigeration unit, a dehumidification rotor, and a carbon capture rotor, a cooling liquid inlet pipeline is fixedly connected between the liquid outlet of the refrigeration unit and the liquid inlet of the upper part of the spray tower, a liquid return circulation pipeline is fixedly connected between the liquid outlet at the bottom of the spray tower and the liquid inlet of the refrigeration unit, and a flue gas outlet is fixedly connected between the upper air outlet of the spray tower and the lower air inlet of the dehumidification rotor. The lower air outlet of the dehumidification wheel and the lower air inlet of the carbon capture wheel are fixedly connected with a flue gas deep dehumidification pipeline, the lower air outlet of the carbon capture wheel and the middle air inlet of the carbon capture wheel are fixedly connected with a carbon capture cooling pipeline, the middle air outlet of the carbon capture wheel and the upper air inlet of the dehumidification wheel are fixedly connected with a desiccant heating pipeline, the upper air outlet of the dehumidification wheel is fixedly connected with an exhaust pipeline, and the upper air outlet of the carbon capture wheel is fixedly connected with a gas compression pipeline.

[0009] The following is a further optimization and / or improvement of one of the above-mentioned technical solutions: The above also includes a multi-stage compressor, a refrigeration liquefaction device, a CO2 storage tank and a flue gas fan. A gas compression pipeline is fixedly connected between the upper air outlet of the carbon capture wheel and the top air inlet of the multi-stage compressor, a CO2 transmission pipeline is fixedly connected between the bottom outlet of the multi-stage compressor and the top inlet of the refrigeration liquefaction device, a CO2 storage pipeline is fixedly connected between the bottom outlet of the refrigeration liquefaction device and the top inlet of the CO2 storage tank, a flue gas boosting pipeline is fixedly connected between the flue gas fan outlet and the lower air inlet of the spray tower, and a flue gas inlet pipeline is fixedly connected to the flue gas fan inlet.

[0010] The above-mentioned dehumidification wheel includes a wheel and a shell. The diameter of the wheel is 300mm to 500mm, and the thickness is 100mm to 500mm. The shell covers the outside of the wheel. The inside of the shell is provided with a first adsorption zone and a first desorption zone. The area ratio of the first adsorption zone to the first desorption zone is 3:1. A flue gas cooling pipeline is fixedly connected between the upper air outlet of the spray tower and the air inlet of the first adsorption zone.

[0011] The above-mentioned carbon capture wheel includes a wheel and a shell. The diameter of the wheel is 500mm to 1000mm, and the thickness is 100mm to 500mm. The shell covers the outside of the wheel. The inside of the shell is provided with a second adsorption zone, a purge zone, a second desorption zone, and a cooling zone in a clockwise direction. The area ratio of the second adsorption zone, the purge zone, the second desorption zone, and the cooling zone is 4:1:3:4. A carbon capture cooling pipeline is fixedly connected between the air outlet of the second adsorption zone and the air inlet of the cooling zone. A desorption heating pipeline is fixedly connected between the air outlet of the cooling zone and the air inlet of the first desorption zone. An exhaust pipeline is fixedly connected to the air outlet of the first desorption zone.

[0012] A primary cooler is fixedly installed on the flue gas cooling pipeline, a secondary cooler is fixedly installed on the carbon capture cooling pipeline, the medium in the cooling liquid inlet pipeline passes through the secondary cooler and the primary cooler in sequence, and a cooling circulation water pump is fixedly installed on the cooling liquid inlet pipeline between the refrigeration unit and the secondary cooler.

[0013] A gas compression pipeline is fixedly connected between the air outlet of the second desorption zone and the air inlet at the top of the multi-stage compressor, a desorption circulation fan is fixedly installed on the gas compression pipeline, a circulation heating desorption pipeline is fixedly connected between the gas compression pipeline between the desorption circulation fan and the multi-stage compressor and the inlet of the second desorption zone, a heater is fixedly installed on the circulation heating desorption pipeline, a purge air inlet pipeline is fixedly connected between the gas compression pipeline between the circulation heating desorption pipeline and the multi-stage compressor and the air inlet of the purge zone, and a purge air outlet pipeline is fixedly connected between the air outlet of the purge zone and the flue gas deep dehumidification pipeline.

[0014] The above-mentioned wheel is a wheel-shaped disc made of rotating fiber material paper, the fiber material is a honeycomb fiber material, and the wheel contains a CO2 adsorbent, wherein the CO2 adsorbent is one or more of 5A, clinoptilolite, silica gel, activated carbon, and MOFs, and the fiber material paper includes ceramic fiber material paper, glass fiber material paper, and carbon fiber material paper.

[0015] The spray tower is one of a packed spray tower, a reactive spray tower and a multi-stage spray tower.

[0016] The above-mentioned spray tower is a multi-stage spray tower.

[0017] The refrigeration unit is one of a compression refrigeration unit, a magnetic suspension refrigeration unit, an absorption refrigeration unit, an evaporative refrigeration unit, a chilled refrigeration unit, and a liquid nitrogen refrigeration unit.

[0018] The above refrigeration unit is a magnetic suspension refrigeration unit.

[0019] The above-mentioned desorption circulation fan is an air-cooled high-temperature resistant centrifugal fan or a water-cooled high-temperature resistant centrifugal fan.

[0020] The heater is one of an electric heater, a gas heater, a steam heater, a hot water heater, and a thermal oil heater.

[0021] The above heater is a thermal oil heater.

[0022] The multi-stage compressor is one of a piston compressor, a screw compressor, a centrifugal compressor and a helical compressor.

[0023] The above-mentioned refrigeration and liquefaction device is one of a compression-type refrigeration and liquefaction device, an absorption-type refrigeration and liquefaction device, a mixed refrigerant refrigeration and liquefaction device, and a heat pump-type refrigeration and liquefaction device.

[0024] The above-mentioned refrigeration liquefaction device is a compression refrigeration liquefaction device using R507 refrigerant.

[0025] The above-mentioned CO2 storage tank is one of a carbon steel storage tank, a stainless steel storage tank, a cryogenic steel storage tank, a composite material storage tank, and a carbon fiber storage tank.

[0026] The above-mentioned CO2 storage tank is a stainless steel storage tank or a cryogenic steel storage tank.

[0027] The second technical solution of the present invention is achieved by the following measures: A method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas comprises the following steps: S1, turn on the flue gas fan, the flue gas is pressurized by the flue gas fan and then transported to the lower part of the spray tower, turn on the refrigeration unit, the cooling liquid generated by the refrigeration unit passes through the secondary cooler, the primary cooler, and the spray tower in sequence, the cooling liquid from top to bottom contacts the flue gas in reverse, the flue gas is discharged after being cooled, and the cooling liquid returns to the refrigeration unit from the bottom of the spray tower for circulation and cooling; S2, the flue gas discharged from the spray tower after cooling is cooled and dehumidified by the first cooler, deeply dehumidified in the first adsorption zone, carbon captured in the second adsorption zone, cooled by the second cooler, cooled in the cooling zone, and heated in the first desorption zone, and then the exhaust gas that meets the emission standards is discharged into the atmosphere; S3, the saturated honeycomb fiber material in the first adsorption zone is rotated to the first desorption zone, and the high-temperature gas in the first desorption zone directly desorbs the saturated honeycomb fiber material, and the desorbed honeycomb fiber material is rotated back to the first adsorption zone for deep dehumidification; S4, the honeycomb fiber material that has been saturated with adsorption in the second adsorption zone is rotated to the purge zone, and the high-concentration CO2 gas in the purge zone discharges the dead volume in the rotor, and then the honeycomb fiber material is rotated to the second desorption zone for cyclic heating and desorption, and finally transferred to the cooling zone for cooling to restore the carbon capture capacity of the carbon capture rotor; S5, after the high-concentration CO2-enriched gas circulated in the second desorption zone is discharged, it is first pressurized by a multi-stage compressor, and then deeply liquefied by a refrigeration and liquefaction device. The obtained liquid CO2 is sent to a CO2 storage tank for storage and standby use.

[0028] The following is a further optimization and / or improvement of the second technical solution of the above invention: In the above step S1, the temperature of the cooling liquid in the spray tower is -10°C to 15°C, and the components in the flue gas include 6% to 17% by volume of CO2, 20% to 60% of water vapor, 30ppm to 200ppm of SO X , 30ppm to 200ppm NO X and particulate matter.

[0029] In the above steps S2, S3 and S4, the adsorption temperatures of the first adsorption zone and the second adsorption zone are both 30°C to 70°C, the desorption temperatures of the first desorption zone and the second desorption zone are both 100°C to 200°C, the rotation speeds of the dehumidification wheel and the carbon capture wheel are both 3r / h to 11r / h, and the flow rates of the flue gas entering the first adsorption zone and the second adsorption zone are both 0.5m / s to 5m / s.

[0030] The present invention has the characteristics of low desorption energy consumption, low gas circulation pressure resistance, continuous process and high heat recovery rate. It increases the enriched CO2 concentration and makes the CO2 concentration in the flue gas after the carbon capture rotor lower. It can achieve a significant reduction in unit CO2 capture energy consumption while ensuring the CO2 removal rate and enrichment concentration. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] Attached Figure 1 This is a schematic diagram of the process flow of Example 1 of the present invention.

[0032] Attached Figure 1 The codes are as follows: 1 for flue gas inlet pipeline, 2 for flue gas pressurization pipeline, 3 for liquid return circulation pipeline, 4 for cooling liquid inlet pipeline, 5 for flue gas cooling pipeline, 6 for flue gas deep dehumidification pipeline, 7 for carbon capture cooling pipeline, 8 for desiccant heating pipeline, 9 for exhaust pipeline, 10 for flue gas fan, 11 for spray tower, 12 for primary cooler, 13 for secondary cooler, 14 for cooling circulation water pump, 15 for refrigeration unit, 16 for gas compression pipeline, 17 for circulation heating Desorption pipeline, 18 is the purge air inlet pipeline, 19 is the CO2 delivery pipeline, 20 is the dehumidification rotor, 21 is the first adsorption zone, 22 is the first desorption zone, 23 is the carbon capture rotor, 24 is the second adsorption zone, 25 is the cooling zone, 26 is the second desorption zone, 27 is the purge zone, 28 is the desorption circulation fan, 29 is the heater, 30 is the multi-stage compressor, 31 is the refrigeration liquefaction device, 32 is the CO2 storage tank, 33 is the CO2 storage pipeline, and 34 is the purge air outlet pipeline. DETAILED DESCRIPTION

[0033] The present invention is not limited by the following embodiments, and specific implementation methods can be determined according to the technical scheme of the present invention and actual conditions. Unless otherwise specified, the various chemical reagents and chemicals mentioned in the present invention are all known and commonly used chemical reagents and chemicals in the prior art.

[0034] The present invention will be further described below in conjunction with embodiments: Embodiment 1: As attached Figure 1As shown, the two-stage rotary adsorption device for capturing carbon dioxide in flue gas comprises a spray tower 11, a refrigeration unit 15, a dehumidification rotary wheel 20, and a carbon capture rotary wheel 23. A cooling liquid inlet pipeline 4 is fixedly connected between the liquid outlet of the refrigeration unit 15 and the upper liquid inlet of the spray tower 11, a liquid return circulation pipeline 3 is fixedly connected between the bottom liquid outlet of the spray tower 11 and the liquid inlet of the refrigeration unit 15, a flue gas cooling pipeline 5 is fixedly connected between the upper air outlet of the spray tower 11 and the lower air inlet of the dehumidification rotary wheel 20, and the dehumidification rotary wheel 23 is fixedly connected between the upper air outlet of the spray tower 11 and the lower air inlet of the dehumidification rotary wheel 20. A flue gas deep dehumidification pipeline 6 is fixedly connected between the lower air outlet of the wheel 20 and the lower air inlet of the carbon capture wheel 23, a carbon capture cooling pipeline 7 is fixedly connected between the lower air outlet of the carbon capture wheel 23 and the middle air inlet of the carbon capture wheel 23, a desiccant heating pipeline 8 is fixedly connected between the middle air outlet of the carbon capture wheel 23 and the upper air inlet of the dehumidification wheel 20, an exhaust pipeline 9 is fixedly connected to the upper air outlet of the dehumidification wheel 20, and a gas compression pipeline 16 is fixedly connected to the upper air outlet of the carbon capture wheel 23.

[0035] Embodiment 2: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, it also includes a multi-stage compressor 30, a refrigeration liquefaction device 31, a CO2 storage tank 32 and a flue gas fan 10. A gas compression pipeline 16 is fixedly connected between the upper air outlet of the carbon capture wheel 23 and the top air inlet of the multi-stage compressor 30, a CO2 delivery pipeline 19 is fixedly connected between the bottom outlet of the multi-stage compressor 30 and the top inlet of the refrigeration liquefaction device 31, and a CO2 storage pipeline 33 is fixedly connected between the bottom outlet of the refrigeration liquefaction device 31 and the top inlet of the CO2 storage tank 32. A flue gas boosting pipeline 2 is fixedly connected between the outlet of the flue gas fan 10 and the lower air inlet of the spray tower 11, and a flue gas inlet pipeline 1 is fixedly connected to the inlet of the flue gas fan 10.

[0036] As needed, the flue gas fan 10 in the present invention adopts one of an axial flow fan, a centrifugal fan, a mixed flow fan, and a back pressure fan, preferably a centrifugal fan of 5kPa to 10kPa, so as to provide pressure to the flue gas to overcome the pressure resistance of subsequent equipment.

[0037] Embodiment 3: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the dehumidification wheel 20 includes a wheel and a shell. The wheel diameter is 300mm to 500mm, and the thickness is 100mm to 500mm. The shell covers the outside of the wheel. The inside of the shell is provided with a first adsorption zone 21 and a first desorption zone 22. The area ratio of the first adsorption zone 21 to the first desorption zone 22 is 3:1. A flue gas cooling pipeline 5 is fixedly connected between the upper air outlet of the spray tower 11 and the air inlet of the first adsorption zone 21.

[0038] Embodiment 4: As an optimization of the above embodiment, as shown in the attached Figure 1As shown, the carbon capture wheel 23 includes a wheel and a shell. The wheel diameter is 500mm to 1000mm, and the thickness is 100mm to 500mm. The shell covers the outer side of the wheel. The inside of the shell is provided with a second adsorption zone 24, a purge zone 27, a second desorption zone 26, and a cooling zone 25 in a clockwise direction. The area ratio of the second adsorption zone 24, the purge zone 27, the second desorption zone 26, and the cooling zone 25 is 4:1:3:4. A carbon capture cooling pipeline 7 is fixedly connected between the air outlet of the second adsorption zone 24 and the air inlet of the cooling zone 25. A desorption heating pipeline 8 is fixedly connected between the air outlet of the cooling zone 25 and the air inlet of the first desorption zone 22. An exhaust pipeline 9 is fixedly connected to the air outlet of the first desorption zone 22.

[0039] As needed, the first adsorption zone 21 in the present invention is mainly used for deep dehydration treatment of flue gas. The desorbed gas of the first desorption zone 22 adopts the outlet flue gas of the cooling zone 25 of the carbon capture wheel 23. Due to the extremely dry characteristics of its flue gas, the desorption of the honeycomb fiber material in the dehumidification wheel 20 is promoted.

[0040] As needed, the dehumidification wheel 20 in the present invention provides dry gas with a dew point below -20°C for the carbon capture wheel 23, so that the adsorbent in the second adsorption zone 24 can adsorb more CO2, and the first desorption zone 22 can reduce the water content of the enriched gas.

[0041] At the same time, the flue gas at the outlet of the second adsorption zone 24 has a relatively low specific heat capacity and an extremely low water content, and as a cooling gas, has a very small effect on reducing the CO2 concentration of the enriched gas.

[0042] Embodiment 5: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, a primary cooler 12 is fixedly installed on the flue gas cooling pipeline 5, a secondary cooler 13 is fixedly installed on the carbon capture cooling pipeline 7, the medium in the cooling liquid inlet pipeline 4 passes through the secondary cooler 13 and the primary cooler 12 in sequence, and a cooling circulation water pump 14 is fixedly installed on the cooling liquid inlet pipeline 4 between the refrigeration unit 15 and the secondary cooler 13.

[0043] As required, both the primary cooler 12 and the secondary cooler 13 need to reduce the flue gas temperature to below zero degrees, so as to provide sufficient cooling capacity for the carbon capture wheel cooling zone 25. The primary cooler 12 and the secondary cooler 13 use one of a shell and tube heat exchanger, a plate heat exchanger, a fin heat exchanger, a spiral plate heat exchanger, and a tube heat exchanger, preferably a plate heat exchanger.

[0044] Embodiment 6: As an optimization of the above embodiment, as shown in the attached Figure 1As shown, a gas compression pipeline 16 is fixedly connected between the air outlet of the second desorption zone 26 and the air inlet at the top of the multi-stage compressor 30, a desorption circulation fan 28 is fixedly installed on the gas compression pipeline 16, a circulation heating desorption pipeline 17 is fixedly connected between the gas compression pipeline 16 between the desorption circulation fan 28 and the multi-stage compressor 30 and the inlet of the second desorption zone 26, a heater 29 is fixedly installed on the circulation heating desorption pipeline 17, a purge inlet pipeline 18 is fixedly connected between the gas compression pipeline 16 between the circulation heating desorption pipeline 17 and the multi-stage compressor 30 and the air inlet of the purge zone 27, and a purge outlet pipeline 34 is fixedly connected between the air outlet of the purge zone 27 and the flue gas deep dehumidification pipeline 6.

[0045] As needed, the heater 29, desorption circulation fan 28 and the second desorption zone 26 in the present invention form a cyclic heating desorption, so that the CO2 desorbed from the honeycomb fiber material of the rotor is continuously enriched into a high-concentration product gas in the circulation pipeline.

[0046] At the same time, the purge of the purge zone 27 can increase the CO2-enriched gas concentration in the circulation pipeline of the second desorption zone 26.

[0047] Example 7: As an optimization of the above example, the rotor is a wheel-shaped disc made by rotating fiber material paper, the fiber material is a honeycomb fiber material, and the rotor contains a CO2 adsorbent, wherein the CO2 adsorbent is one or more of 5A, clinoptilolite, silica gel, activated carbon, and MOFs, and the fiber material paper includes ceramic fiber material paper, glass fiber material paper, and carbon fiber material paper.

[0048] According to the needs, the CO2 adsorbent in the present invention can be a variety of combinations, which can form a gradient distribution of pore size, so that the adsorbent coating has two advantages, one is the adsorption depth of micropores that are quickly filled, and the other is the large adsorption capacity of macropores that gradually capture CO2.

[0049] At the same time, the honeycomb porous structure of the honeycomb fiber material in the rotor and the multiple adsorbent combination coating further reduce the desorption temperature of the carbon capture rotor 23, and the optimal desorption temperature is 120℃ to 140℃; the honeycomb porous structure reduces the flue gas pressure resistance and improves the heat and mass transfer coefficient of the rotor honeycomb adsorbent, so that the rotor can achieve excellent characteristics of rapid desorption and adsorption, and the multiple adsorbent combination coating effectively reduces the desorption activation energy of the adsorbed CO2. Therefore, the dual support of structure and material can make the desorption temperature of the carbon capture rotor 23 lower than the desorption temperature of the traditional granular bed.

[0050] Embodiment 8: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the spray tower 11 is one of a packed spray tower, a reactive spray tower, and a multi-stage spray tower.

[0051] Embodiment 9: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the spray tower 11 is a multi-stage spray tower.

[0052] As needed, the multi-stage spray tower in the present invention adopts direct evaporation to efficiently cool the flue gas to room temperature, and the cooling liquid comes from the refrigeration unit 15. The cooling liquid in the refrigeration unit 15 can be industrial water, pure water, or ethylene glycol solution, and the ethylene glycol solution can be cooled to below zero degrees using refrigeration equipment, which can achieve a better cooling effect.

[0053] Embodiment 10: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the refrigeration unit 15 is one of a compression refrigeration unit, a magnetic suspension refrigeration unit, an absorption refrigeration unit, an evaporative refrigeration unit, a chilled refrigeration unit, and a liquid nitrogen refrigeration unit.

[0054] Embodiment 11: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the refrigeration unit 15 is a magnetic suspension refrigeration unit.

[0055] According to the needs, the present invention sequentially provides cooling liquid for the second stage cooler 13, the first stage cooler 12, and the spray tower 11, and realizes circulating refrigeration, which further expands the selection of refrigeration liquid. At the same time, the magnetic suspension refrigeration unit is preferred, which has lower energy consumption and a refrigeration temperature below -5°C.

[0056] Embodiment 12: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the desorption circulation fan 28 is an air-cooled high-temperature resistant centrifugal fan or a water-cooled high-temperature resistant centrifugal fan.

[0057] Since the gas needs to be continuously heated and transported to the second desorption zone 26, the desorption circulation fan 28 is used to provide sufficient power for the circulating gas while also providing a higher air supply pressure to accelerate the desorption process.

[0058] As required, the desorption circulation fan 28 may preferably be a water-cooled high-temperature resistant centrifugal fan, and the inlet and outlet of the desorption circulation fan 28 need to be insulated.

[0059] Embodiment 13: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the heater 29 is one of an electric heater, a gas heater, a steam heater, a hot water heater, and a thermal oil heater.

[0060] Embodiment 14: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the heater 29 is a thermal oil heater.

[0061] The heating temperature of the heater 29 is 120° C. to 140° C. as required.

[0062] Embodiment 15: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the multi-stage compressor 30 is one of a piston compressor, a screw compressor, a centrifugal compressor, and a helical compressor.

[0063] According to needs, a centrifugal compressor should be selected for high-flow product gas output; a piston compressor should be selected for low-flow product gas output; the main function is to reduce the liquefaction temperature of CO2.

[0064] Embodiment 16: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the refrigeration liquefaction device 31 is one of a compression type refrigeration liquefaction device, an absorption type refrigeration liquefaction device, a mixed refrigerant refrigeration liquefaction device, and a heat pump type refrigeration liquefaction device.

[0065] Embodiment 17: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the refrigeration liquefaction device 31 is a compression refrigeration liquefaction device using R507 refrigerant.

[0066] Embodiment 18: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the CO2 storage tank 32 is one of a carbon steel storage tank, a stainless steel storage tank, a cryogenic steel storage tank, a composite material storage tank, and a carbon fiber storage tank.

[0067] Embodiment 19: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, the CO2 storage tank 32 is a stainless steel storage tank or a cryogenic steel storage tank. Since the temperature of the liquefied CO2 is relatively low, a stainless steel storage tank or a cryogenic steel storage tank is used for storage.

[0068] As required, the pipelines and equipment of the two-stage rotary adsorption device for capturing carbon dioxide in flue gas may be provided with conventional valves, thermometers, pressure gauges, etc. known and used in the art according to production needs.

[0069] Embodiment 20: As attached Figure 1 As shown, the method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas comprises the following steps: S1, turn on the flue gas fan 10, the flue gas is pressurized by the flue gas fan 10 and then transported to the lower part of the spray tower 11, turn on the refrigeration unit 15, the cooling liquid generated by the refrigeration unit 15 passes through the secondary cooler 13, the primary cooler 12, and the spray tower 11 in sequence, the cooling liquid contacts the flue gas from top to bottom in reverse, the flue gas is discharged after being cooled, and the cooling liquid returns to the refrigeration unit 15 from the bottom of the spray tower 11 for circulation and cooling; S2, the flue gas discharged from the spray tower 11 is cooled and dehumidified by the primary cooler 12, deeply dehumidified by the first adsorption zone 21, carbon captured by the second adsorption zone 24, cooled by the secondary cooler 13, cooled by the cooling zone 25, and heated by the first desorption zone 22, and then the exhaust gas that meets the emission standards is discharged into the atmosphere; S3, the saturated honeycomb fiber material in the first adsorption zone 21 is rotated to the first desorption zone 22, and the high-temperature gas in the first desorption zone 22 directly desorbs the saturated honeycomb fiber material, and the desorbed honeycomb fiber material is rotated back to the first adsorption zone 21 for deep dehumidification; S4, the honeycomb fiber material that has been saturated with adsorption in the second adsorption zone 24 is rotated to the purge zone 27, and the high-concentration CO2 gas in the purge zone 27 discharges the dead volume in the rotor, and then the honeycomb fiber material is rotated to the second desorption zone 26 for cyclic heating and desorption, and finally transferred to the cooling zone 25 for cooling to restore the carbon capture capacity of the carbon capture rotor 23; S5, after the high-concentration CO2-enriched gas circulated in the second desorption zone 26 is discharged, it is first pressurized by a multi-stage compressor 30, and then deeply liquefied by a refrigeration liquefaction device 31, and the obtained liquid CO2 is sent to a CO2 storage tank 32 for storage and standby use.

[0070] Embodiment 21: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, in step S1, the temperature of the cooling liquid in the spray tower 11 is -10°C to 15°C, and the components in the flue gas include 6% to 17% by volume of CO2, 20% to 60% of water vapor, 30ppm to 200ppm of SO X , 30ppm to 200ppm NO X and particulate matter.

[0071] Embodiment 22: As an optimization of the above embodiment, as shown in the attached Figure 1 As shown, in steps S2, S3 and S4, the adsorption temperatures of the first adsorption zone 21 and the second adsorption zone 24 are both 30°C to 70°C, the desorption temperatures of the first desorption zone 22 and the second desorption zone 26 are both 100°C to 200°C, the rotation speeds of the dehumidification wheel 20 and the carbon capture wheel 23 are both 3r / h to 11r / h, and the flow rates of the flue gas entering the first adsorption zone 21 and the second adsorption zone 24 are both 0.5m / s to 5m / s.

[0072] The first purpose of the present invention is to provide a two-stage rotary adsorption device for capturing carbon dioxide in flue gas. The flue gas is introduced by a flue gas fan 10, first cooled and dehumidified by a spray tower 11 and a cooler, then dehumidified by a dehumidification rotary wheel 20 and carbon captured by a carbon capture rotary wheel 23, and finally high-purity CO2 liquid is transported to a CO2 storage tank 32 through a multi-stage compressor 30 and a refrigeration liquefaction device 31.

[0073] The second object of the present invention is to provide a method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas, which can realize the process of first dehumidifying the flue gas and then capturing carbon by setting a two-stage rotary wheel (i.e., a dehumidification rotary wheel 20 and a carbon capture rotary wheel 23); in the present invention, the dew point of the flue gas after the dehumidification rotary wheel 20 is relatively low, so that the carbon capture rotary wheel 23 adsorbs less water and increases the enriched CO2 concentration; the CO2 concentration of the flue gas after the carbon capture rotary wheel 23 of the present invention is relatively low, which is mainly due to the fact that the structure of the honeycomb fiber material in the carbon capture rotary wheel 23 is coated with a CO2 high-performance adsorption material.

[0074] The present invention successfully achieves continuous and efficient carbon dioxide capture and treatment of large-volume flue gas by introducing a two-stage rotor design, and the CO2 removal rate can reach more than 90%. At the same time, combined with the self-circulating thermal desorption of the dehumidification rotor 20 and the carbon capture rotor 23, the present invention can produce no less than 90% of CO2 product gas for subsequent CO2 liquefaction and storage. Therefore, the present invention not only improves the heat recovery efficiency, but also significantly reduces the heat energy consumption during the desorption process.

[0075] Compared with the prior art, the present invention has the following beneficial effects: (1) The present invention can realize the continuous capture and recovery of large-scale flue gas CO2, significantly reduce the operating cost of the process, and realize large-scale low-energy capture of CO2; (2) The present invention sets up a two-stage rotor (i.e., a dehumidification rotor 20 and a carbon capture rotor 23) in series, and the dehumidification rotor 20 can provide extremely low dew point flue gas for the carbon capture rotor 23, and effectively reduce the moisture content of the enriched gas in the desorption zone of the carbon capture rotor 23; (3) The present invention designs a spray tower 11, a primary cooler 12, and a secondary cooler 13 as a flue gas cooling treatment, thereby increasing the adsorption capacity of the CO2 adsorbent in the rotor and improving the CO2 removal rate of the system; (4) The present invention provides a self-circulating thermal desorption device in the carbon capture rotor 23, so that the high-temperature enriched gas is heated and used for desorption again, the desorption heat utilization rate and recovery rate are high, and the CO2 product gas concentration is higher, and the capture energy consumption is lower than that of the general rotor adsorption technology, wherein the desorption gas flow comes from part of the enriched gas and part of the cooling outlet gas; (5) The honeycomb fiber material used in the rotor of the present invention has a honeycomb porous structure and a combination coating of multiple adsorbents, which improves the heat and mass transfer coefficient of the rotor material and the CO2 adsorption capacity, reduces the desorption activation energy and desorption temperature, and can achieve desorption at a relatively low temperature of 120°C to 140°C; (6) The present invention does not generate waste byproducts or emit fugitive substances during operation, nor does it pose significant risks to the environment, health or safety.

[0076] Example 23: As shown in the attached Figure 1 As shown, the method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas comprises the following steps: S1, turn on the flue gas fan 10, the flue gas (mainly composed of 12% CO2, 70% relative humidity, 60ppm NOx, 70ppm SOx, and the rest N2 and O2) is 700Nm 3 The inlet flow of / h is increased in pressure by the flue gas fan 10 and then transported to the lower part of the spray tower 11. The refrigeration unit 15 (the cooling liquid is a -10°C ethylene glycol solution) is turned on. The cooling liquid generated by the refrigeration unit 15 passes through the secondary cooler 13, the primary cooler 12, and the spray tower 11 in sequence. The cooling liquid contacts the flue gas from top to bottom in reverse direction. The flue gas is discharged after being cooled. The cooling liquid returns to the refrigeration unit 15 from the bottom of the spray tower 11 for circulation cooling. S2, the flue gas discharged from the spray tower 11 after cooling and dehumidification in the primary cooler 12, deep dehumidification in the first adsorption zone 21, carbon capture in the second adsorption zone 24, cooling in the secondary cooler 13, cooling in the cooling zone 25, and heating in the first desorption zone 22, is discharged into the atmosphere after obtaining tail gas that meets the emission standards, wherein the CO2 concentration of the flue gas after decarbonization is below 5000ppm; S3, the saturated honeycomb fiber material in the first adsorption zone 21 is rotated to the first desorption zone 22, and the high-temperature gas in the first desorption zone 22 directly desorbs the saturated honeycomb fiber material, and the desorbed honeycomb fiber material is rotated back to the first adsorption zone 21 for deep dehumidification; S4, the honeycomb fiber material that has been saturated with adsorption in the second adsorption zone 24 is rotated to the purge zone 27, and the high-concentration CO2 gas in the purge zone 27 discharges the dead volume in the wheel, and then the honeycomb fiber material is rotated to the second desorption zone 26 for cyclic heating and desorption, and finally transferred to the cooling zone 25 for cooling to restore the carbon capture capacity of the carbon capture wheel 23, wherein the dehumidification wheel 20 has a diameter of 550 mm, a thickness of 300 mm, and a rotation speed of 6 r / h, the carbon capture wheel 23 has a diameter of 960 mm, a thickness of 500 mm, and a rotation speed of 6 r / h, the CO2 adsorbent on the dehumidification wheel 20 and the carbon capture wheel 23 is a combination of 5A, clinoptilolite, and silica gel, the desorption temperatures of the first desorption zone 22 and the second desorption zone 26 are both 120°C, and the circulating desorption gas flow rate during cyclic heating and desorption in the second desorption zone 26 is 250 Nm 3 / h; S5, after the high-concentration CO2-enriched gas circulated in the second desorption zone 26 is discharged, it is first pressurized by a multi-stage compressor 30, and then deeply liquefied by a refrigeration liquefaction device 31 (the refrigeration temperature is -25°C). The obtained liquid CO2 is sent to a CO2 storage tank 32 for storage and standby use. The flow rate of the high-concentration CO2-enriched gas circulated and discharged from the second desorption zone 26 is 20Nm 3 / h.

[0077] The dead volume in S4 is the gap in the honeycomb channel of the rotor, which contains raw gas. If it is not purged, it will affect the concentration of the desorbed gas.

[0078] Example 24: The method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas, the other operating steps are consistent with the method steps described in Example 23, except that: in step S1, the flue gas is heated at 300 Nm 3 The flue gas enters with an inlet flow rate of / h and the CO2 concentration in the flue gas is 6%.

[0079] Example 25: The method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas, the other operating steps are consistent with the method steps described in Example 23, except that: in step S1, the flue gas is heated at 1000 Nm 3 / h inlet flow rate enters, and the cooling liquid in the refrigeration unit 15 is industrial water at 5°C.

[0080] Example 26: The method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas, the other operating steps are consistent with the method steps described in Example 23, except that: in step S4, the circulating desorption gas flow rate is 100Nm 3 / h.

[0081] Example 27: The method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas, the other operating steps are consistent with the method steps described in Example 23, except that: in step S4, the circulating desorption gas flow rate is 500Nm when the second desorption zone 26 performs cyclic heating desorption 3 / h.

[0082] Comparative Example 1: The other operating steps are consistent with the method steps described in Example 23, except that: in step S2, the dehumidification wheel 20 is removed from the two-stage rotary adsorption device for capturing carbon dioxide in flue gas, that is, the second adsorption zone 24 of the carbon capture rotary wheel 23 is directly introduced after the primary cooler 12.

[0083] The CO2 adsorption amount, recovery rate, concentration and energy consumption in the flue gas during the treatment process of Examples 23 to 27 and Comparative Example 1 were tested and compared, and the results are shown in Table 1.

[0084] Table 1 .

[0085] From Table 1, we can see that (1) The honeycomb fiber material of the dehumidification wheel 20 and the carbon capture wheel 23 of the present invention can still maintain a dew point of -20°C and a CO2 exhaust concentration of less than 0.5% after multiple cycles.

[0086] (2) The present invention can achieve low-concentration CO2 enrichment to more than 90%, and the carbon capture energy consumption is no more than 1.8 GJ / tCO2.

[0087] (3) Flue gas with a higher inlet flow rate will slightly reduce the CO2 adsorption capacity of the rotor. This is mainly due to the rapid heat and mass transfer coefficient of the adsorbent in the honeycomb fiber material of the rotor, which reduces the adsorption penetration time. However, the rotor speed is too slow and the adsorbent has reached the adsorption saturation state when entering the desorption zone.

[0088] (4) The dehumidification wheel 20 is an indispensable device in the present invention. The absence of the dehumidification wheel 20 will reduce the CO2 enrichment concentration of the device.

[0089] In summary, the present invention has the characteristics of low desorption energy consumption, low gas circulation pressure resistance, continuous process and high heat recovery rate. It increases the enriched CO2 concentration and makes the CO2 concentration in the flue gas after the carbon capture rotor lower. It can achieve a significant reduction in unit CO2 capture energy consumption while ensuring the CO2 removal rate and enrichment concentration.

[0090] The above technical features constitute the embodiments of the present invention, which have strong adaptability and implementation effect. Non-essential technical features can be added or reduced according to actual needs to meet the requirements of different situations.

Claims

1. A two-stage rotary adsorption device for capturing carbon dioxide in flue gas, characterized in that It includes a spray tower, a refrigeration unit, a dehumidification wheel, and a carbon capture wheel. A cooling liquid inlet pipeline is fixedly connected between the liquid outlet of the refrigeration unit and the upper liquid inlet of the spray tower, a liquid return circulation pipeline is fixedly connected between the bottom liquid outlet of the spray tower and the liquid inlet of the refrigeration unit, a flue gas cooling pipeline is fixedly connected between the upper air outlet of the spray tower and the lower air inlet of the dehumidification wheel, a flue gas deep dehumidification pipeline is fixedly connected between the lower air outlet of the dehumidification wheel and the lower air inlet of the carbon capture wheel, a carbon capture cooling pipeline is fixedly connected between the lower air outlet of the carbon capture wheel and the middle air inlet of the carbon capture wheel, a desiccant heating pipeline is fixedly connected between the middle air outlet of the carbon capture wheel and the upper air inlet of the dehumidification wheel, an exhaust pipeline is fixedly connected to the upper air outlet of the dehumidification wheel, and a gas compression pipeline is fixedly connected to the upper air outlet of the carbon capture wheel.

2. The double-stage rotary adsorption device for capturing carbon dioxide in flue gas according to claim 1 is characterized in that It also includes a multi-stage compressor, a refrigeration liquefaction device, a CO2 storage tank and a flue gas fan. A gas compression pipeline is fixedly connected between the upper air outlet of the carbon capture wheel and the top air inlet of the multi-stage compressor, a CO2 transmission pipeline is fixedly connected between the bottom outlet of the multi-stage compressor and the top inlet of the refrigeration liquefaction device, a CO2 storage pipeline is fixedly connected between the bottom outlet of the refrigeration liquefaction device and the top inlet of the CO2 storage tank, a flue gas boosting pipeline is fixedly connected between the flue gas fan outlet and the lower air inlet of the spray tower, and a flue gas inlet pipeline is fixedly connected to the flue gas fan inlet.

3. The two-stage rotary adsorption device for capturing carbon dioxide in flue gas according to claim 1 or 2, characterized in that The dehumidification wheel includes a wheel and a shell. The diameter of the wheel is 300mm to 500mm, and the thickness is 100mm to 500mm. The shell covers the outside of the wheel. The inside of the shell is provided with a first adsorption zone and a first desorption zone. The area ratio of the first adsorption zone to the first desorption zone is 3:

1. A flue gas cooling pipeline is fixedly connected between the upper air outlet of the spray tower and the air inlet of the first adsorption zone.

4. The double-stage rotary adsorption device for capturing carbon dioxide in flue gas according to claim 3 is characterized in that The carbon capture wheel includes a wheel and a shell. The wheel has a diameter of 500mm to 1000mm and a thickness of 100mm to 500mm. The shell covers the outside of the wheel. The inside of the shell is provided with a second adsorption zone, a purge zone, a second desorption zone and a cooling zone in a clockwise direction. The area ratio of the second adsorption zone, the purge zone, the second desorption zone and the cooling zone is 4:1:3:

4. A carbon capture cooling pipeline is fixedly connected between the air outlet of the second adsorption zone and the air inlet of the cooling zone. A desorption heating pipeline is fixedly connected between the air outlet of the cooling zone and the air inlet of the first desorption zone. An exhaust pipeline is fixedly connected to the air outlet of the first desorption zone.

5. The double-stage rotary adsorption device for capturing carbon dioxide in flue gas according to claim 4 is characterized in that A primary cooler is fixedly installed on the flue gas cooling pipeline, a secondary cooler is fixedly installed on the carbon capture cooling pipeline, the medium in the cooling liquid inlet pipeline passes through the secondary cooler and the primary cooler in sequence, and a cooling circulation water pump is fixedly installed on the cooling liquid inlet pipeline between the refrigeration unit and the secondary cooler.

6. The double-stage rotary adsorption device for capturing carbon dioxide in flue gas according to claim 5, characterized in that A gas compression pipeline is fixedly connected between the air outlet of the second desorption zone and the air inlet on the top of the multi-stage compressor, a desorption circulation fan is fixedly installed on the gas compression pipeline, a circulating heating desorption pipeline is fixedly connected between the gas compression pipeline between the desorption circulation fan and the multi-stage compressor and the inlet of the second desorption zone, a heater is fixedly installed on the circulating heating desorption pipeline, a purge inlet pipeline is fixedly connected between the gas compression pipeline between the circulating heating desorption pipeline and the multi-stage compressor and the air inlet of the purge zone, and a purge outlet pipeline is fixedly connected between the air outlet of the purge zone and the flue gas deep dehumidification pipeline.

7. The double-stage rotary adsorption device for capturing carbon dioxide in flue gas according to claim 6, characterized in that The rotor is a wheel-shaped disc made of rotating fiber material paper, the fiber material is a honeycomb fiber material, and the rotor contains a CO2 adsorbent, wherein the CO2 adsorbent is one or more of 5A, clinoptilolite, silica gel, activated carbon, and MOFs, and the fiber material paper includes ceramic fiber material paper, glass fiber material paper, and carbon fiber material paper; or / and, the spray tower is one of a packed spray tower, a reactive spray tower, and a multi-stage spray tower; or / and, the refrigeration unit is one of a compression refrigeration unit, a magnetic levitation refrigeration unit, an absorption refrigeration unit, an evaporative refrigeration unit, a chilled refrigeration unit, and a liquid nitrogen refrigeration unit; or / and, the desorption The circulating fan is an air-cooled high-temperature resistant centrifugal fan or a water-cooled high-temperature resistant centrifugal fan; or / and, the heater is an electric heater, a gas heater, a steam heater, a hot water heater, and a thermal oil heater; or / and, the multi-stage compressor is a piston compressor, a screw compressor, a centrifugal compressor, and a spiral compressor; or / and, the refrigeration and liquefaction device is a compression refrigeration and liquefaction device, an absorption refrigeration and liquefaction device, a mixed refrigerant refrigeration and liquefaction device, and a heat pump refrigeration and liquefaction device; or / and, the CO2 storage tank is a carbon steel storage tank, a stainless steel storage tank, a low-temperature steel storage tank, a composite material storage tank, and a carbon fiber storage tank.

8. The double-stage rotary adsorption device for capturing carbon dioxide in flue gas according to claim 7, characterized in that The spray tower is a multi-stage spray tower; or / and, the refrigeration unit is a magnetic levitation refrigeration unit; or / and, the heater is a thermal oil heater; or / and, the refrigeration liquefaction device is a compression refrigeration liquefaction device using R507 refrigerant; or / and, the CO2 storage tank is a stainless steel storage tank or a low-temperature steel storage tank.

9. A method for implementing the two-stage rotary adsorption device for capturing carbon dioxide in flue gas according to any one of claims 1 to 8, characterized in that The steps include: S1, turn on the flue gas fan, the flue gas is pressurized by the flue gas fan and then transported to the lower part of the spray tower, turn on the refrigeration unit, the cooling liquid generated by the refrigeration unit passes through the secondary cooler, the primary cooler, and the spray tower in sequence, the cooling liquid from top to bottom contacts the flue gas in reverse, the flue gas is discharged after being cooled, and the cooling liquid returns to the refrigeration unit from the bottom of the spray tower for circulation and cooling; S2, the flue gas discharged from the spray tower after cooling is cooled and dehumidified by the first cooler, deeply dehumidified in the first adsorption zone, carbon captured in the second adsorption zone, cooled by the second cooler, cooled in the cooling zone, and heated in the first desorption zone, and then the exhaust gas that meets the emission standards is discharged into the atmosphere; S3, the saturated honeycomb fiber material in the first adsorption zone is rotated to the first desorption zone, and the high-temperature gas in the first desorption zone directly desorbs the saturated honeycomb fiber material, and the desorbed honeycomb fiber material is rotated back to the first adsorption zone for deep dehumidification; S4, the honeycomb fiber material that has been saturated with adsorption in the second adsorption zone is rotated to the purge zone, and the high-concentration CO2 gas in the purge zone discharges the dead volume in the rotor, and then the honeycomb fiber material is rotated to the second desorption zone for cyclic heating and desorption, and finally transferred to the cooling zone for cooling to restore the carbon capture capacity of the carbon capture rotor; S5, after the high-concentration CO2-enriched gas circulated in the second desorption zone is discharged, it is first pressurized by a multi-stage compressor, and then deeply liquefied by a refrigeration and liquefaction device. The obtained liquid CO2 is sent to a CO2 storage tank for storage and standby use.

10. The method for implementing a two-stage rotary adsorption device for capturing carbon dioxide in flue gas according to claim 9, characterized in that In step S1, the temperature of the cooling liquid in the spray tower is -10°C to 15°C, and the components in the flue gas include 6% to 17% CO2, 20% to 60% water vapor, 30ppm to 200ppm SO X , 30ppm to 200ppm NO X and particulate matter; or / and, in steps S2, S3 and S4, the adsorption temperatures of the first adsorption zone and the second adsorption zone are both 30°C to 70°C, the desorption temperatures of the first desorption zone and the second desorption zone are both 100°C to 200°C, the rotation speeds of the dehumidification wheel and the carbon capture wheel are both 3r / h to 11r / h, and the flow rates of the flue gas entering the first adsorption zone and the second adsorption zone are both 0.5m / s to 5m / s.

Images