In-situ regeneration system and method for directly capturing air and taking water from air

Abstract

The invention discloses an in-situ regeneration system and an in-situ regeneration method for directly capturing and taking water from air, and the in-situ regeneration system for directly capturing and taking water from air takes water from air while capturing carbon by a DAC (Digital-to-Analog Converter), and realizes in-situ action of low-temperature steam of a water adsorbent on a carbon dioxide adsorbent for desorption. Heat loss in the external steam conveying process is eliminated, the steam utilization efficiency is greatly improved, and meanwhile in-situ steam assists desorption of the carbon dioxide adsorbent so that the vacuum degree requirement in the regeneration process can be lowered.

Description

Technical Field

[0001] The present invention belongs to the technical field of carbon capture, and specifically relates to a direct air capture collaborative air water extraction in-situ regeneration system and method. Background Art

[0002] Currently, although traditional carbon dioxide (CO2) capture, utilization, and storage (CCUS) technologies can already achieve partial decarbonization of large-scale power and industrial point sources, carbon emissions from dispersed sources in industries such as agriculture and transportation still cause the concentration of CO2 in the air to continuously increase.

[0003] DAC technology, i.e., the direct air capture (Direct Air Capture) technology of carbon dioxide. Compared with traditional CCUS technologies, DAC technology can be flexibly applied to locations with abundant renewable energy such as solar energy and wind energy, thereby offsetting the energy consumption required in the DAC process and reducing operating costs. However, existing DAC solutions still face bottleneck problems such as high energy consumption, low regeneration efficiency, and insufficient steam utilization, and their large-scale application is severely restricted.

[0004] In DAC technology, solid adsorption technology is the most promising due to its advantages such as simple operation process, low regeneration temperature (80 - 120 °C), and environmental friendliness. In recent years, significant progress has been made in the application of this technology in the fields of adsorbent material development and system integration optimization. However, before achieving large-scale deployment and application, the direct air capture system by solid adsorption method still needs to solve the following key problems: (1) Limited by moisture and low-concentration CO2 (about 420 ppm) in the air, water in the air often competes with CO2 for adsorption, resulting in the inactivation of most commercial adsorbents; (2) Under the actual large-scale air capture working conditions, the high pressure drop required in a conventional packed fixed bed will greatly increase the energy consumption of the fan; (3) In the DAC scheme using vacuum pressure swing adsorption process, a high-vacuum pump group will cause huge energy consumption; while the DAC scheme using steam regeneration requires a stable high-temperature steam source, which also poses higher requirements for the CO2 adsorption selectivity and stability of the adsorbent; (4) In areas lacking electricity, it is difficult to deploy DAC technology and there is insufficient flexibility.

[0005] Generally speaking, the development of DAC technology is still in its infancy, with high energy consumption and costs remaining high. Therefore, developing new DAC solid adsorption technologies with low energy consumption and low costs is the top priority at present. Summary of the Invention

[0006] In view of the problems existing in the prior art, the present invention provides a direct air capture collaborative air water extraction in-situ regeneration system and method, which extracts water from the air while capturing carbon by DAC, reduces the vacuum degree requirement in the regeneration process through in-situ steam assistance, and combines solar power generation energy storage power supply to reduce energy consumption.

[0007] In one aspect, the present invention provides a direct air capture collaborative air water extraction in-situ regeneration system, which includes an adsorption / desorption module, a fan module, a cooling module, and a product collection module;

[0008] The adsorption / desorption module includes two or more boxes and adsorbent units placed in the boxes. Two opposite sides of the box are open, and a sealing frame is installed at the outer edge of each open, and a sealing plate that can move left and right is installed by means of the sealing frame; the width of the sealing plate is equal to or slightly larger than the width of the box; a product output pipeline is also provided at the top of the box, and the rear end of the product output pipeline is connected to a vacuum pump;

[0009] The fan module is disposed opposite to one open of the box, includes one or more fans, the number of which is the same as that of the boxes and corresponds to the boxes one by one;

[0010] The cooling module is connected to the vacuum pump at the rear end of the product output pipeline of the adsorption / desorption module through a pipeline;

[0011] The product collection module is connected to the cooling module through a pipeline, and includes a gas-liquid separator and a carbon dioxide storage tank and a water storage tank connected to the rear end thereof.

[0012] Preferably, a carbon dioxide detector is provided on the inner wall of the fan.

[0013] In one or more embodiments, the system is configured with a power supply module, and the power supply module uses an existing power system or adopts a solar power generation energy storage system.

[0014] In one or more embodiments, the sealing plate installed on the sealing frame can be electrically controlled, manually controlled, or both.

[0015] In one or more embodiments, the adsorbent unit includes a plurality of adsorption thin layers, and the adsorption thin layer is configured with a thermostat or a programmable logic controller; each adsorption thin layer is composed of an electric heating wire mesh loaded with a main adsorbent, a secondary adsorbent, or a main adsorbent and a secondary adsorbent; the main adsorbent is an air carbon dioxide adsorbent, and the secondary adsorbent is an air water adsorbent.

[0016] Preferably, the air carbon dioxide adsorbent is an amine-modified porous adsorbent.

[0017] More preferably, the method for amine modification is selected from one or more of physical impregnation method, chemical grafting method, and in-situ synthesis method.

[0018] More preferably, the amine is selected from one or more of polyethyleneimine, polypropyleneimine, diethanolamine, diethylenetriamine, triethylenetetramine, and tetraethylenepentamine.

[0019] More preferably, the porous adsorbent is selected from one or more of mesoporous silica, activated carbon, alumina, zeolite, metal-organic frameworks (MOFs), and porous organic polymers (POPs).

[0020] More preferably, the air carbon dioxide adsorbent is selected from triethylenetetramine grafted styrene resin, polyethyleneimine impregnated SBA-15, and polyethyleneimine impregnated MIL-101(Cr).

[0021] Preferably, the air water adsorbent is selected from one or more of silica gel, alumina, molecular sieve, activated carbon, montmorillonite desiccant, fiber-based desiccant, superabsorbent resin, and hydrogel.

[0022] Preferably, the material of the electric heating wire mesh is nickel-chromium alloy.

[0023] Preferably, the mesh number of the electric heating wire mesh can be flexibly selected according to the characteristics of the adsorbent.

[0024] Preferably, the adsorbent unit includes 1 to 100 adsorption thin layers. More preferably, the adsorbent unit includes 15 to 50 adsorption thin layers.

[0025] In one or more embodiments, the ratio range of the air carbon dioxide adsorbent to the air water adsorbent in the adsorbent unit is (1 to 9):1.

[0026] In one or more embodiments, each adsorption thin layer is composed of an electric heating wire mesh loaded with a main adsorbent or a secondary adsorbent. The adsorption thin layers are placed in parallel and arranged vertically. All the adsorption thin layers loaded with the main adsorbent are located above all the adsorption thin layers loaded with the secondary adsorbent, or the adsorption thin layers loaded with the main adsorbent and the adsorption thin layers loaded with the secondary adsorbent are alternately placed.

[0027] In one or more embodiments, each adsorption thin layer is composed of an electric heating wire mesh loaded with a main adsorbent and a secondary adsorbent. The adsorption thin layers are placed in parallel and arranged vertically.

[0028] In one or more embodiments, a fixed distance of 0.1 to 100 mm is provided between adjacent adsorption thin layers. More preferably, a fixed distance of 0.5 to 2 mm is provided between adjacent adsorption thin layers.

[0029] In another aspect, the present invention provides the application of the direct air capture collaborative air water extraction in-situ regeneration system as described in any embodiment herein in carbon capture.

[0030] In another aspect, the present invention provides a method for carbon dioxide capture, the method comprising using the direct air capture collaborative air water extraction in-situ regeneration system as described in any embodiment herein.

[0031] In one or more embodiments, a blower is used to control the air flow rate input into the adsorption / desorption module to be 0.01 - 10 m / s.

[0032] Preferably, a blower is used to control the air flow rate input into the system to be 1 - 3 m / s.

[0033] In one or more embodiments, the time of the adsorption process is 1 min - 24 h.

[0034] Preferably, the time of the adsorption process is 5 - 10 h.

[0035] In one or more embodiments, the temperature of the desorption process is 55 - 130 °C, the pressure of the desorption process is 5 - 55 kPa, the time of the desorption process is 0.5 - 2.5 h, and the cooling time after desorption is 1 min - 6 h.

[0036] Preferably, the temperature of the desorption process is 60 - 120 °C.

[0037] Preferably, the pressure of the desorption process is 10 - 50 kPa.

[0038] Preferably, the time of the desorption process is 0.5 - 1 h.

[0039] Preferably, the cooling time after desorption is 0.3 - 0.7 h.

[0040] The direct air capture collaborative air water extraction in-situ regeneration system and method provided by the present invention have at least the following beneficial effects compared with the prior art:

[0041] 1. Multi-layer adsorption bed in-situ steam regeneration technology: A hierarchical adsorption bed structure is constructed inside the adsorption module. By adjusting the proportion and spatial position of the carbon dioxide adsorbent and the water adsorbent, the low-temperature steam of the water adsorbent acts on the carbon dioxide adsorbent for desorption in-situ, eliminating the heat loss during the external steam transportation process, and greatly improving the steam utilization efficiency;

[0042] 2. Flexible adaptation of multi-morphology materials and heating elements: The heating mode based on the stainless steel electric heating plate / electric heating mesh box is compatible with various morphological adsorbent structures, achieving uniform heat generation throughout the adsorbent layer, and further reducing the heat loss of the system;

[0043] 3. Modular and scalable architecture design: Standardized direct air capture unit modules are adopted, and a matrix capture array is formed through three-dimensional spatial arrangement and combination. The spatial limitation of the traditional DAC system is broken through modular reconstruction ability, and parallel expansion of the thermal system and the power system is supported;

[0044] 4. Full-cycle solar energy empowerment: Double-sided photovoltaic modules are integrated on the top of the device. The generated electric energy directly drives the operation of the fan, the release of water vapor, and the enrichment of carbon dioxide by the vacuum pump. The proportion of renewable energy in the whole process exceeds 80%. The present invention relies on the deep coupling of solar power generation and steam regeneration, enabling the system to have the ability to operate independently in remote areas or distributed scenarios, and providing an innovative solution for the rapid deployment of 10,000-ton DAC plants. Brief Description of the Drawings

[0045] Figure 1 It is a composition diagram of a direct air capture collaborative air water extraction in-situ regeneration system.

[0046] Figure 2 It is a structural diagram of the adsorption / desorption module.

[0047] Figure 3 It is a front view of the adsorption / desorption module.

[0048] Figure 4 It is a composition diagram of a direct air capture collaborative air water extraction in-situ regeneration system coupled with a solar power generation energy storage system.

[0049] Figure 5 It is a structural diagram of the adsorption thin layer in the adsorbent unit.

[0050] Figure 6 It is a schematic diagram of the adsorption and desorption processes of the adsorbent unit. Among them, Figure 6 A in Figure 6 is a schematic diagram of the adsorption process;

[0051] Description of the figure numbers:

[0052] Adsorption / desorption module 10, box body 11, adsorbent unit 12, open end 13, sealing frame 14, sealing plate 15, product output pipeline 16, handle 17, vacuum pump 18, fan module 20, fan 21, cooling module 30, product collection module 40, gas-liquid separator 41, carbon dioxide storage tank 42, water storage tank 43, solar power generation energy storage system 50, solar panel 51, inverter 52, monitoring system 53, adsorption thin layer 121. Detailed Embodiments

[0053] As Figure 1As shown in the figure, this embodiment is a direct air capture collaborative air water extraction in-situ regeneration system, including an adsorption / desorption module 10, a fan module 20, a cooling module 30, and a product collection module 40, where:

[0054] As Figure 2 and Figure 3 As shown in the figure, the adsorption / desorption module 10 includes two or more boxes 11 and adsorbent units 12 placed in the boxes 11. Two opposite sides of the box 11 are openings 13. A sealing frame 14 is installed at the outer edge of each opening 13, and a sealing plate 15 that can move left and right is installed by means of the sealing frame 14; the width of the sealing plate 15 is equal to or slightly larger than the width of the box 11, so that when the sealing plate 14 moves to one side of the opening 13, it can seal a corresponding adsorbent unit 12, but will not simultaneously seal another adjacent box 11; a product output pipeline 16 is further provided at the top of the box 11, and the rear end of the product output pipeline 16 is connected to a vacuum pump 18, which is used to output products (CO2 and water vapor) when the corresponding adsorbent unit 12 is desorbed.

[0055] The fan module 20 is arranged facing an opening 13 of the box 11, and includes one or more fans 21, the number of which is the same as that of the boxes 11 and corresponds to the boxes 11 one by one, and is used to convey air to the adsorbent units 12 in the boxes 11. Preferably, the fan 21 is an intelligent variable frequency fan, which can adaptively adjust the power according to the external real-time air flow rate, the adsorption kinetics of the adsorbent, and the tightness of the adsorbent filling, so that the air flow rate input into the system is 1 - 3 m / s. More preferably, two fan modules 20 are configured, which are respectively arranged facing the two side openings 13 of the box 11, so as to adjust the opened fan module 20 to reduce energy consumption when the wind direction of the external environment changes. Further, a carbon dioxide detector (not shown in the figure) is provided on the inner wall of the fan 21, which is used to detect the carbon dioxide concentration in the input air.

[0056] The cooling module 30 is connected to the vacuum pump 18 at the rear end of the product output pipeline 16 of the adsorption / desorption module 10 through a pipeline, and is used to condense the water vapor in the output products into water. Preferably, the cooling device 30 includes a cold trap.

[0057] The product collection module 40 is connected to the cooling module 30 through a pipeline, and includes a gas-liquid separator 41 and a carbon dioxide storage tank 42 and a water storage tank 43 connected to the rear end thereof. The gas-liquid separator 41 is used to separate CO2 and condensed water, so as to store them through the carbon dioxide storage tank 42 and the water storage tank 43 respectively.

[0058] Furthermore, the direct air capture and air water extraction in-situ regeneration system of the present invention is also equipped with a power supply module, which can use the existing power system or the like. Figure 4 As shown, a solar power generation and energy storage system 50 is used.

[0059] The solar power generation and energy storage system 50 includes a solar panel 51, an inverter 52, a monitoring system 53 and an energy storage battery 54. The solar panel 51 can be selected from existing known products, such as monocrystalline silicon cells or polycrystalline silicon cells. The inverter 52 is used to convert direct current into alternating current to power electrical components in the system, such as the wind turbine 21. The monitoring system 53 includes sensors, data collectors, monitoring panels, etc., which are used to monitor the operating status parameters of the solar power generation and energy storage module 50 in real time, including the power generation power, voltage, and current of the solar panel 51, the working status of the inverter 52, the ambient temperature, light intensity, etc., to ensure a stable and reliable energy supply. The composition and operation of the monitoring system 53 are known in the prior art and will not be described in detail here.

[0060] Furthermore, the sealing plate 15 mounted on the sealing frame 14 can be electrically controlled, manually controlled, or both. For example, a connection hole can be provided on one side of the sealing plate 15 and a bearing can be installed therein. A screw hole can be provided on the corresponding side of the sealing frame 14. A handle 17 with a screw rod can be inserted through the screw hole of the sealing frame 14 and then fixed to the bearing in the sealing plate 15. Rotating the handle 17 or electrically driving the handle 17 can cause the screw rod to rotate in conjunction with the rotation, thereby driving the sealing plate 15 to move left and right along the sealing frame 14.

[0061] Further, if Figure 5 As shown, the adsorbent unit 12 includes a plurality of adsorption thin layers 121, preferably 1 to 100, and the adsorption thin layers 121 are equipped with a temperature controller or a programmable logic controller (not shown in the figure). Each adsorption thin layer 121 is composed of an electric heating wire mesh loaded with a primary adsorbent, a secondary adsorbent, or a primary adsorbent and a secondary adsorbent. The primary adsorbent is an air carbon dioxide adsorbent, and the secondary adsorbent is an air water adsorbent. The primary adsorbent is used to adsorb carbon dioxide from the air, and the secondary adsorbent is used to adsorb moisture from the air.

[0062] Furthermore, the ratio of the air carbon dioxide adsorbent to the air water adsorbent in the adsorbent unit 12 is in the range of (1-9):1.

[0063] Further, each adsorption thin layer 121 is composed of an electrothermal wire mesh loaded with a main adsorbent or a secondary adsorbent. The adsorption thin layers 121 are arranged in parallel and vertically. All the adsorption thin layers 121 loaded with the main adsorbent are located above all the adsorption thin layers 121 loaded with the secondary adsorbent, or the adsorption thin layers 121 loaded with the main adsorbent and the adsorption thin layers 121 loaded with the secondary adsorbent are arranged alternately.

[0064] Further, a fixed spacing of 0.2 - 3 mm is provided between adjacent adsorption thin layers 121. The electrothermal wire mesh is used to heat the main adsorbent, the secondary adsorbent, or both the main adsorbent and the secondary adsorbent; the form of the electrothermal wire mesh is an electrothermal wire mesh box or an electrothermal wire mesh plate, and the mesh number of the electrothermal wire mesh can be flexibly selected according to the characteristics of the adsorbent. The electrothermal wire mesh box is a cuboid or a cube, and its six faces are all composed of electrothermal wire meshes. The pore diameter of the electrothermal wire mesh is smaller than the particle size of the main adsorbent or the secondary adsorbent.

[0065] During the operation of the system, when desorption of the adsorbent unit 12 is required, under the monitoring and adjustment of the temperature controller or the programmable logic controller, the electrothermal wire mesh is started to heat the main adsorbent or the secondary adsorbent, so that the temperature of the adsorbent unit 12 to be desorbed is maintained at 60 - 120 °C.

[0066] Further, the material of the electrothermal wire mesh includes but is not limited to nickel-chromium alloy (Ni-Cr), iron-chromium-aluminum alloy (Fe-Cr-Al), copper-nickel alloy (Cu-Ni), etc.

[0067] In the present invention, two or more adsorbent units 12 in the adsorption / desorption module 10 can be alternately switched between the adsorption mode and the desorption mode, that is: when an adsorbent unit 12 is saturated with adsorption, it is switched to the desorption mode, and at the same time, other adsorbent units 12 are started for adsorption. After being saturated with adsorption, they are switched to the desorption mode. At the same time, the adsorbent units 12 that have completed desorption and cooling are switched to the adsorption mode, and so on alternately. Preferably, each adsorbent unit 12 in the adsorption / desorption module 10 is independently powered, so that a single adsorbent unit 12 can be heated for desorption.

[0068] During desorption, the sealing doors 15 of the sealing frames 14 on both sides of the box body 11 move to one side of the corresponding adsorbent unit 12, forming a relatively sealed space in the area of the adsorbent unit 12. Then, the vacuum pump 18 is turned on, and the gas in the space is extracted through the product output pipeline 16, so that the pressure in the space is maintained at 10 - 50 kPa. Under the heating effect of the electric heating wire mesh and the action of the vacuum pump, the extracted gas includes CO2 desorbed from the main adsorbent and water vapor desorbed from the secondary adsorbent (the adsorbed water is released in the form of water vapor). Based on the specific design of the main adsorbent and the secondary adsorbent, the water vapor desorbed from the secondary adsorbent can assist in reducing the partial pressure of carbon dioxide in the desorption module, thereby promoting the desorption and regeneration of carbon dioxide, which is beneficial to reducing the energy consumption of the vacuum pump 18.

[0069] Furthermore, the air carbon dioxide adsorbent is an amine-modified porous adsorbent. This type of adsorbent has a relatively high adsorption specificity for carbon dioxide; in addition, the co-promoting effect of carbon dioxide and water in a humid environment is beneficial to the improvement of the working capacity of this type of adsorbent.

[0070] Furthermore, the method of amine modification is selected from one or more of physical impregnation method, chemical grafting method, and in-situ synthesis method. Furthermore, the amine includes one or more of polyethyleneimine, polypropyleneimine, diethanolamine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, and other compounds with amino functional groups.

[0071] Furthermore, the porous adsorbent is selected from one or more of mesoporous silica, activated carbon, alumina, zeolite, metal-organic framework (MOFs), and porous organic polymer (POPs).

[0072] Furthermore, the types of air water absorbents include but are not limited to one or more of silica gel, alumina, molecular sieve, activated carbon, montmorillonite desiccant, fiber-based desiccant, superabsorbent resin, and hydrogel.

[0073] Preferably, the amine-modified porous adsorbent is selected from one or more of triethylenetetramine-grafted polystyrene-based resin, polyethyleneimine-impregnated polystyrene-based resin, tetraethylenepentamine-grafted polystyrene-based resin, polyethyleneimine-impregnated MIL-1*01*(Cr), and polyethyleneimine-impregnated SBA-15.

[0074] In one or more embodiments, the working principle of the direct air capture and synergistic air water extraction in-situ regeneration system of this embodiment is as follows:

[0075] First, start the fan module 20 to radially transport air to the adsorption / desorption module 10; the fan 21 adaptively adjusts the fan power according to the real-time air flow rate, the adsorption kinetics of the adsorbent, and the packing density of the adsorbent, so that the air enters the adsorbent unit 12 of the adsorption / desorption module 10 radially at a flow rate of 1 - 3 m / s for the adsorption of carbon dioxide and water. The adsorption process is as shown in Figure 6 A shown in. In the air, carbon dioxide and water are adsorbed by the adsorbent unit 12, and the decarbonized gas after adsorption is directly discharged from the other side of the adsorbent unit 12.

[0076] When the adsorption thin layer 121 of the adsorbent unit 12 reaches a relatively saturated carbon dioxide adsorption degree and needs to be desorbed, close the corresponding fan 21, move the sealing plates 15 on both sides to the corresponding sides of the adsorbent unit 12 to form a relatively sealed space in the area of the adsorbent unit 12. At this time, start the vacuum pump 18 connected to the adsorbent unit 12 to extract the gas in the sealed space, maintain the pressure in the space at 10 - 50 kPa, and use a temperature controller or a programmable logic controller to heat the adsorption thin layer 121 in the box to start the desorption process, thereby completing the switching from the adsorption mode to the desorption mode. The desorption process is as shown in Figure 6 B shown in. Under the action of the electric heating wire mesh and the vacuum pump 18, the adsorbed water is released in the form of water vapor, acting in situ on the adsorption thin layer 121 of the adsorbent unit 12 to promote the desorption of the adsorbed carbon dioxide. In addition, the water vapor desorbed from the adsorbent can assist in reducing the carbon dioxide partial pressure in the desorption module, further promoting the desorption and regeneration of carbon dioxide, and reducing the energy consumption of the vacuum pump 18. While the adsorbent unit 12 switches from the adsorption mode to the desorption mode, the adjacent adsorbent unit 12 starts the adsorption mode, and the corresponding fan 21 transports air to it for the adsorption of carbon dioxide and water.

[0077] When the desorption of the adsorption thin layer 121 is completed, close the vacuum pump 18 connected to the box 11 corresponding to the adsorbent unit 12, stop heating the adsorption thin layer 121, and let the adsorption thin layer 121 cool naturally; after the cooling is completed, start the inlet fan 21 corresponding to the box 11 to switch to the adsorption mode and start the adsorption process, thereby completing the functional conversion from the desorption mode to the adsorption mode.

[0078] By alternately switching between two or more adsorbent units 12 in the adsorption mode and the desorption mode, continuous operation of the system can be achieved.

[0079] Finally, as shown in Figure 1 and Figure 2 shown, the gas desorbed from the adsorbent unit 12 passes through the product output pipeline 16, and after the water vapor in it is condensed into liquid water through a cold trap, it enters the product collection module 40 for collection.

[0080] Example 1

[0081] Each of the left and right boxes 11 of the adsorption / desorption module 2 is filled with 15 adsorption thin layers 121. Each adsorption thin layer 121 is composed of a 60-mesh nickel-chromium alloy electrothermal wire mesh box loaded with triethylenetetramine grafted polystyrene-based resin (main adsorbent) or activated alumina (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 3:1; the adsorption thin layers 121 are placed in parallel and arranged vertically, and the distance between the adsorption thin layers 121 is 1 mm. All the adsorption thin layers 121 loaded with the main adsorbent are located above all the adsorption thin layers 121 loaded with the secondary adsorbent.

[0082] During system operation, the fan stabilizes the external air flow rate at about 1 m / s and then introduces it into the direct air capture and air-water harvesting in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 6 h, and the decarbonized gas after adsorption is directly discharged from the other side of the adsorbent unit 12. After the adsorption is completed, the function is switched from the adsorption mode to the desorption mode, and desorption begins. During the desorption process, the electrothermal wire mesh of the adsorbent unit 12 is gradually heated to 100 °C, and a vacuum pump 18 is used to maintain the pressure in the desorption module at about 30 kPa. The desorption time is 1 h. The carbon dioxide and water desorbed are passed through the product output pipeline 16, and after the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After the desorption is completed, the desorption module is cooled for 0.5 h.

[0083] After measurement, in a single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 57%, and the system energy consumption is 860 kWh / tCO2.

[0084] Example 2

[0085] Each of the left and right boxes 11 of the adsorption / desorption module 2 is filled with 15 adsorption thin layers 121. Each adsorption thin layer 121 is composed of a 60-mesh nickel-chromium alloy electrothermal wire mesh box loaded with polyethyleneimine-impregnated polystyrene-based resin (main adsorbent) or silica gel (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 9:1; the adsorption thin layers 121 are placed in parallel and arranged vertically, and the distance between the adsorption thin layers 121 is 2 mm. All the adsorption thin layers 121 loaded with the main adsorbent are located above all the adsorption thin layers 121 loaded with the secondary adsorbent.

[0086] When the system is running, the fan stabilizes the external air flow rate at about 1 m / s and then introduces it into the direct air capture and air water extraction in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 10 h. After adsorption, the decarbonized gas is directly discharged from the other side of the adsorbent unit 12. After the adsorption is completed, the function is switched from the adsorption mode to the desorption mode. During the desorption process, the electrothermal wire mesh of the adsorbent unit 12 is gradually heated up to 120 °C, and a vacuum pump 18 is used to maintain the pressure in the desorption module at about 10 kPa. The desorption time is 0.5 h. The desorbed carbon dioxide and water pass through the product output pipeline 16. After the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After the desorption is completed, the desorption module is cooled for 0.5 h.

[0087] After measurement, in a single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 44%, and the system energy consumption is 1065 kWh / tCO2.

[0088] Example 3

[0089] In the left and right boxes 11 of the adsorption / desorption module 2, 50 adsorption thin layers 121 are filled respectively. Each adsorption thin layer 121 consists of a 60-mesh nickel-chromium alloy electrothermal wire mesh box loaded with triethylenetetramine grafted polystyrene resin (main adsorbent) or activated alumina (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 1:1; each adsorption thin layer 121 is placed in parallel and arranged vertically, and the distance between the adsorption thin layers 221 is 0.5 mm. The adsorption thin layers 121 loaded with the main adsorbent and the adsorption thin layers 121 loaded with the secondary adsorbent are placed alternately.

[0090] When the system is running, the fan stabilizes the external air flow rate at about 1 m / s and then introduces it into the direct air capture and air water extraction in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 6 h. After adsorption, the decarbonized gas is directly discharged from the other side of the adsorbent unit 12. After the adsorption is completed, the function is switched from the adsorption mode to the desorption mode. During the desorption process, the electrothermal wire mesh of the adsorbent unit 12 is gradually heated up to 100 °C, and a vacuum pump 18 is used to maintain the pressure in the desorption module at about 50 kPa. The desorption time is 1 h. The desorbed carbon dioxide and water pass through the product output pipeline 16. After the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After the desorption is completed, the desorption module is cooled for 0.5 h.

[0091] After measurement, in a single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 63%, and the system energy consumption is 785 kWh / tCO2.

[0092] Example 4

[0093] Each of the left and right boxes 11 of the adsorption / desorption module 2 is filled with 50 adsorption thin layers 121. Each adsorption thin layer 121 is composed of a 60-mesh nickel-chromium alloy electric heating wire mesh box loaded with tetraethylenepentamine grafted polystyrene-based resin (main adsorbent) or silica gel (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 1:1; each adsorption thin layer 121 is placed in parallel and arranged vertically, and the distance between the adsorption thin layers 121 is 0.5 mm. All the adsorption thin layers 121 loaded with the main adsorbent are located above all the adsorption thin layers 121 loaded with the secondary adsorbent.

[0094] When the system operates, the fan stabilizes the external air flow rate at about 1 m / s and then introduces it into the direct air capture and air-water harvesting in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 6 h, and the decarbonized gas after adsorption is directly discharged from the other side of the adsorbent unit 12. After the adsorption is completed, the sealing plate 26 of the inlet / outlet sliding seal valve is moved and adjusted to the adsorption module to swap the adsorption module and the desorption module. During the desorption process, the electric heating wire mesh of the adsorbent unit 12 is gradually heated to 100 °C, and the vacuum pump 18 is used to maintain the pressure in the desorption module at about 50 kPa. The desorption time is 1 h. The carbon dioxide and water desorbed are passed through the product output pipeline 16, and after the water vapor therein is condensed into liquid water via the cold trap, they enter the product collection module 40 for collection. After the desorption is completed, the desorption module is cooled for 0.5 h.

[0095] After measurement, in a single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 59%, and the system energy consumption is 812 kWh / tCO2.

[0096] Example 5

[0097] Each of the left and right boxes 11 of the adsorption / desorption module 2 is filled with 15 adsorption thin layers 121. Each adsorption thin layer 121 is composed of a 60-mesh nickel-chromium alloy electric heating wire mesh box loaded with triethylenetetramine grafted polystyrene-based resin (main adsorbent) or activated alumina (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 3:1; each adsorption thin layer 121 is placed in parallel and arranged vertically, and the distance between the adsorption thin layers is 2 mm. All the adsorption thin layers 121 loaded with the main adsorbent are located above all the adsorption thin layers 121 loaded with the secondary adsorbent. The inlet fan is an intelligent variable-frequency fan.

[0098] During system operation, the fan stabilizes the external air flow rate at about 2 m / s and then introduces it into the direct air capture and air-water harvesting in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 5 h, and the decarbonized gas after adsorption is directly discharged from the other side of the adsorbent unit 12. After the adsorption is completed, a function switch from the adsorption mode to the desorption mode is carried out. During the desorption process, the electrothermal wire mesh of the adsorbent unit 12 is gradually heated to 100 °C, and a vacuum pump 18 is used to maintain the pressure in the desorption module at about 30 kPa. The desorption time is 1 h. The desorbed carbon dioxide and water pass through the product output pipeline 16, and after the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After the desorption is completed, the desorption module is cooled for 0.5 h.

[0099] After measurement, in a single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 32%, and the system energy consumption is 984 kWh / tCO2.

[0100] Example 6

[0101] In the left and right boxes 11 of the adsorption / desorption module 2, each is filled with 50 adsorption thin layers 121. Each adsorption thin layer 121 consists of a 60-mesh nickel-chromium alloy electrothermal wire mesh box loaded with polyethyleneimine-impregnated polystyrene-based resin (main adsorbent) or silica gel (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 9:1; the adsorption thin layers 121 are placed in parallel and vertically arranged, and the spacing between the adsorption thin layers 121 is 0.5 mm. The adsorption thin layers 121 loaded with the main adsorbent and the adsorption thin layers 121 loaded with the secondary adsorbent are alternately placed.

[0102] During system operation, the fan stabilizes the external air flow rate at about 1 m / s and then introduces it into the direct air capture and air-water harvesting in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 10 h, and the decarbonized gas after adsorption is directly discharged from the other side of the adsorbent unit 12. After the adsorption is completed, a function switch from the adsorption mode to the desorption mode is carried out. During the desorption process, the electrothermal wire mesh of the adsorbent unit 12 is gradually heated to 120 °C, and under the action of a vacuum pump 18, the pressure in the desorption module is maintained at about 10 kPa. The desorption time is 0.5 h. The desorbed carbon dioxide and water pass through the product output pipeline 16, and after the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After the desorption is completed, the desorption module is cooled for 0.5 h.

[0103] After measurement, in a single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 46%, and the system energy consumption is 931 kWh / tCO2.

[0104] Example 7

[0105] Each of the left and right boxes 11 of the adsorption / desorption module 2 is filled with 50 adsorption thin layers 121. Each adsorption thin layer 121 consists of a 60-mesh nickel-chromium alloy electric heating wire mesh box loaded with polyethyleneimine-impregnated polystyrene-based resin (main adsorbent) or silica gel (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 9:1; the adsorption thin layers 121 are placed in parallel and vertically arranged, and the distance between the adsorption thin layers 121 is 0.5 mm. The adsorption thin layers 121 loaded with the main adsorbent and the adsorption thin layers 121 loaded with the secondary adsorbent are placed alternately.

[0106] During system operation, the fan stabilizes the external air flow rate at about 3 m / s and then introduces it into the direct air capture and air water extraction in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 5 h, and the decarbonized gas after adsorption is directly discharged from the other side of the adsorbent unit 12. After adsorption, the function is switched from the adsorption mode to the desorption mode. During the desorption process, the electric heating wire mesh of the adsorbent unit 12 is gradually heated to 100 °C, and a vacuum pump 18 is used to maintain the pressure in the desorption module at about 10 kPa. The desorption time is 1 h. The desorbed carbon dioxide and water pass through the product output pipeline 16, and after the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After desorption, the desorption module is cooled for 0.5 h.

[0107] After measurement, in a single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 24%, and the system energy consumption is 1189 kWh / tCO2.

[0108] Example 8

[0109] Each of the left and right boxes 11 of the adsorption / desorption module is filled with 50 adsorption thin layers 121. Each adsorption thin layer 121 consists of a 60-mesh nickel-chromium alloy electric heating wire mesh box loaded with polyethyleneimine-impregnated MIL-101(Cr) (main adsorbent) or silica gel (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 3:1; the adsorption thin layers 121 are placed in parallel and vertically arranged, and the distance between the adsorption thin layers 121 is 0.5 mm. The adsorption thin layers 121 loaded with the main adsorbent and the adsorption thin layers 121 loaded with the secondary adsorbent are placed alternately.

[0110] During system operation, the fan stabilizes the external air flow rate at about 1 m / s and then introduces it into the direct air capture and air water extraction in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 5 h. After adsorption, the decarbonized gas is directly discharged from the other side of the adsorbent unit 12. After adsorption is completed, the sealing plate 26 of the inlet / outlet sliding seal valve is moved and adjusted to the adsorption module to swap the adsorption module and the desorption module. During the desorption process, the electrothermal wire mesh of the adsorbent unit 12 is gradually heated up to 80 °C, and a vacuum pump 18 is used to maintain the pressure in the desorption module at about 30 kPa. The desorption time is 1 h. The desorbed carbon dioxide and water pass through the product output pipeline 16, and after the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After desorption is completed, the desorption module is cooled for 0.5 h.

[0111] After measurement, in a single adsorption-desorption process using the above solution, the capture rate of carbon dioxide in the air is 65%, and the system energy consumption is 794 kWh / tCO2.

[0112] Example 9

[0113] Each of the left and right boxes 11 of the adsorption / desorption module 2 is filled with 50 adsorption thin layers 121. Each adsorption thin layer 121 consists of a 60-mesh nickel-chromium alloy electrothermal wire mesh box loaded with polyethyleneimine-impregnated SBA-15 (main adsorbent) or silica gel (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 9:1; each adsorption thin layer 121 is placed in parallel and arranged vertically, and the spacing between the adsorption thin layers 121 is 0.5 mm. All the adsorption thin layers 121 loaded with the main adsorbent are located above all the adsorption thin layers 121 loaded with the secondary adsorbent.

[0114] During system operation, the fan stabilizes the external air flow rate at about 2 m / s and then introduces it into the direct air capture and air water extraction in-situ regeneration system. During the adsorption process, air is continuously introduced into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 5 h. After adsorption, the decarbonized gas is directly discharged from the other side of the adsorbent unit 12. After adsorption is completed, a functional switch from the adsorption mode to the desorption mode is carried out. During the desorption process, the electrothermal wire mesh of the adsorbent unit 12 is gradually heated up to 80 °C, and under the action of a vacuum pump 18, the pressure in the desorption module is maintained at about 10 kPa. The desorption time is 1 h. The desorbed carbon dioxide and water pass through the product output pipeline 16, and after the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After desorption is completed, the desorption module is cooled for 0.5 h.

[0115] After measurement, in the single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 30%, and the system energy consumption is 952 kWh / tCO2.

[0116] Example 10

[0117] In the left and right boxes 11 of the adsorption / desorption module 2, 20 adsorption thin layers 121 are filled respectively. Each adsorption thin layer 121 consists of a 60-mesh nickel-chromium alloy electrothermal wire mesh box loaded with triethylenetetramine grafted polystyrene resin (main adsorbent) or activated alumina (secondary adsorbent); the ratio of the main adsorbent to the secondary adsorbent is 9:1; each adsorption thin layer 121 is placed parallel and vertically arranged, the spacing between the adsorption thin layers is 0.5 mm, and the adsorption thin layers 121 loaded with the main adsorbent and the adsorption thin layers 121 loaded with the secondary adsorbent are placed alternately.

[0118] When the system is running, the fan stabilizes the external air flow rate at about 1 m / s, and then passes it into the direct air capture and air-water extraction in-situ regeneration system. During the adsorption process, air is continuously passed into one of the boxes 11 for the adsorption of carbon dioxide and water. The adsorption time is 6 h, and the decarbonized gas after adsorption is directly discharged from the other side of the adsorbent unit 12. After the adsorption is completed, the function is switched from the adsorption mode to the desorption mode. During the desorption process, the electrothermal wire mesh of the adsorbent unit 12 is gradually heated to 60 °C, and a vacuum pump is used to maintain the pressure in the desorption module at about 10 kPa. The desorption time is 1 h. The carbon dioxide and water desorbed are passed through the product output pipeline 16, and after the water vapor therein is condensed into liquid water via a cold trap, they enter the product collection module 40 for collection. After the desorption is completed, the desorption module is cooled for 0.5 h.

[0119] After measurement, in the single adsorption-desorption process using the above scheme, the capture rate of carbon dioxide in the air is 67%, and the system energy consumption is 843 kWh / tCO2.

Claims

1. A direct air capture and air water extraction in-situ regeneration system, characterized in that: The system includes an adsorption / desorption module (10), a fan module (20), a cooling module (30) and a product collection module (40); The adsorption / desorption module (10) comprises two or more boxes (11) and an adsorbent unit (12) placed in the boxes (11); two opposite sides of the boxes (11) are open (13); a sealing frame (14) is installed at the outer edge of each opening (13); and a sealing plate (15) that can move left and right is installed with the aid of the sealing frame (14); the width of the sealing plate (15) is equal to or slightly larger than the width of the boxes (11); a product output pipe (16) is also provided on the top of the boxes (11), and a vacuum pump (18) is connected to the rear end of the product output pipe (16); The fan module (20) is arranged facing an opening (13) of the box (11), and includes one or more fans (21), the number of which is the same as the box (11) and corresponds one to one with the box (11); The cooling module (30) is connected to the vacuum pump (18) at the rear end of the product output pipeline (16) of the adsorption / desorption module (10) through a pipeline; The product collection module (40) is connected to the cooling module (30) via a pipeline, and comprises a gas-liquid separator (41) and a carbon dioxide storage tank (42) and a water storage tank (43) connected to its rear end.

2. The direct air capture and air water extraction in-situ regeneration system according to claim 1, characterized in that: The system is equipped with a power supply module, which uses an existing power system or a solar power generation and energy storage system (50).

3. The direct air capture and air water extraction in-situ regeneration system according to claim 1, characterized in that: The adsorbent unit (12) comprises a plurality of adsorption thin layers (121), and the adsorption thin layers (121) are equipped with a temperature controller or a programmable logic controller; each adsorption thin layer (121) is composed of an electric heating wire mesh loaded with a primary adsorbent, a secondary adsorbent, or a primary adsorbent and a secondary adsorbent; the primary adsorbent is an air carbon dioxide adsorbent, and the secondary adsorbent is an air water adsorbent.

4. The direct air capture and air water extraction in-situ regeneration system according to claim 3, characterized in that: The ratio of the air carbon dioxide adsorbent to the air water adsorbent in the adsorbent unit (12) is in the range of (1-9):

1.

5. The direct air capture and air-water in-situ regeneration system according to claim 3, characterized in that: Each adsorption thin layer (121) is composed of an electric heating wire mesh loaded with a main adsorbent or a secondary adsorbent. The adsorption thin layers (121) are placed in parallel and arranged vertically. All adsorption thin layers (121) loaded with the main adsorbent are located above all adsorption thin layers (121) loaded with the secondary adsorbent, or the adsorption thin layers (121) loaded with the main adsorbent and the adsorption thin layers (121) loaded with the secondary adsorbent are placed alternately.

6. The direct air capture and air water extraction in-situ regeneration system according to claim 3, characterized in that: A fixed spacing of 0.1 to 100 mm is provided between adjacent adsorption thin layers (121).

7. Application of the direct air capture combined with air water extraction in-situ regeneration system according to any one of claims 1 to 6 in carbon capture.

8. A method for capturing carbon dioxide, characterized in that: The method comprises using the direct air capture combined with air-water in-situ regeneration system according to any one of claims 1 to 6.

9. The method for capturing carbon dioxide according to claim 8, wherein: A fan (21) is used to control the air flow rate input into the adsorption / desorption module to 0.01 to 10 m / s.

10. The method for capturing carbon dioxide according to claim 8, wherein: The temperature of the desorption process is 55-130° C., and the pressure of the desorption process is 5-55 kPa.

Images