A low energy air continuous carbon capture test system and method of operation

Abstract

The application discloses a kind of low energy consumption air continuous carbon capture test system and operating method, equipment energy consumption system includes adsorption device and fan, heating energy consumption system includes desorption device, the desorption device is heat fluid jacket type, process energy consumption system includes regenerative adsorbent delivery pipe and pneumatic conveying road pipe, the application utilizes adsorption device fan two purposes, the jacket intercommunication of desorption device and regenerative adsorbent delivery pipe, desorption device part product gas heating cycle, bunker and adsorption device integrated combination measure, reach the equipment energy consumption of adsorbent regeneration stage, reduce the heating energy consumption of adsorbent desorption stage, simplify adsorption device and reduce the process energy consumption of adsorption stage, realize the overall low energy consumption operation of large-scale air continuous carbon dioxide capture test system, on the basis of simplifying carbon capture process flow, by reducing desorption process energy consumption and effectively utilizing regenerative process heat, realize the low energy consumption operation of air continuous carbon capture whole system.

Description

Technical Field

[0001] This invention belongs to the field of power plant flue gas carbon dioxide capture technology, specifically relating to a low-energy-consumption continuous air carbon capture test system and its operation method. Background Technology

[0002] Direct air capture (DAC) is considered an irreplaceable negative emission technology. Among its methods, adsorption has become a hot topic due to its advantages such as low cost, chemical stability, and high CO2 selectivity. The principle is to selectively adsorb CO2 molecules onto the surface of an adsorbent using weak van der Waals forces or strong covalent bonds. Different regeneration methods are used depending on the adsorption mechanism, thereby releasing the adsorbed CO2 and achieving air carbon capture.

[0003] Compared to fixed-bed adsorption processes, in fluidized-bed systems, adsorbent particles can move at different speeds within the system. After adsorption saturation, they can be further regenerated, thus achieving the recycling of adsorbents through repeated adsorption, desorption, and regeneration. For example, temperature-switched adsorption of CO2 involves adsorption at lower temperatures (40-60℃) and desorption at higher temperatures (80-150℃).

[0004] Currently, continuous operation is gradually replacing the intermittent operation of traditional fixed-bed systems. However, the overall energy consumption of the system is difficult to reduce. This is mainly because the adsorbent desorption process requires heat and even a certain degree of vacuum, while the adsorbent regeneration process requires lowering the temperature and restoring the adsorbent's environmental conditions. Many factors influence the energy demand in these processes. Implementing heat supply systems or integrating heat recovery and other heat exchange methods is difficult to achieve in various application scenarios, and their complexity makes them clearly impractical. Summary of the Invention

[0005] To address the problems existing in the prior art, the present invention aims to provide a low-energy-consumption continuous air carbon capture test system and operation method. Based on simplifying the carbon capture process, the system achieves low-energy-consumption operation of the entire continuous air carbon capture system by reducing energy consumption in the desorption process and effectively utilizing heat in the regeneration process.

[0006] This invention is achieved through the following technical solution:

[0007] A low-energy-consumption continuous carbon capture system for air includes,

[0008] Equipment energy consumption system, heating energy consumption system and process energy consumption system;

[0009] The energy consumption system of the equipment includes an adsorption device and an induced draft fan, wherein the air outlet of the adsorption device is connected to the inlet of the induced draft fan.

[0010] The heating energy consumption system includes a desorption device, which is a hot fluid jacket type. A jacket is provided on the outer wall of the desorption device. The top and bottom of the jacket are separated by a partition. The interior of the jacket is a heat exchange fluid. The adsorbent inlet of the desorption device is connected to the adsorbent outlet of the adsorption device.

[0011] The process energy consumption system includes a regenerated adsorbent delivery pipe and a pneumatic delivery pipe. The adsorbent outlet of the desorption device is connected to one end of the regenerated adsorbent delivery pipe, and the other end of the regenerated adsorbent delivery pipe is connected to the adsorption device.

[0012] The regenerated adsorbent delivery pipe is a jacketed type, and a second jacket is provided on the outside of the regenerated adsorbent delivery pipe. The second jacket is separated radially by a second partition. One outlet of the induced draft fan is connected to the pneumatic delivery pipe.

[0013] Preferably, the adsorption device includes, from top to bottom, a hopper section, an adsorption section, and an adsorption saturation section. A gas-solid separation section is provided on the top of one side of the hopper section. The inlet of the hopper section is connected to the regenerated adsorbent conveying pipe. The adsorption saturation section is connected to the adsorbent inlet of the desorption device. The outlet of the gas-solid separation section is connected to the hopper exhaust port.

[0014] Preferably, the adsorption device has a cylindrical structure and is supported by a metal bracket; the outer wall of the adsorption section has a metal mesh annular structure, and the adsorbent is filled in the annular structure to form an adsorbent layer.

[0015] Preferably, the heating energy consumption system further includes a heater; the top of the desorption device is provided with a product gas CO2 outlet pipe, a branch of the product gas CO2 outlet pipe is connected to the inlet of the heater, and the outlet of the heater is connected to the desorption device through a hot gas outlet pipe to form a circulation loop.

[0016] Preferably, a ball valve is provided at the inlet of the heater.

[0017] Preferably, the heat exchange fluid is low-quality water.

[0018] Preferably, a regulating valve is installed on the pipeline between the outlet of the induced draft fan and the pneumatic conveying pipeline.

[0019] Preferably, the adsorbent outlet of the adsorption device is provided with an adsorption device discharge valve.

[0020] Preferably, the outlet of the induced draft fan is connected to the outside air.

[0021] An operating method for a low-energy-consumption continuous carbon capture test system for air, comprising:

[0022] The adsorbent enters the adsorption device and, under its own weight, accumulates and slowly descends. Simultaneously, air, driven by a fan, enters from around the adsorption device's cylinder and comes into full contact with the adsorbent. The active groups on the adsorbent capture low concentrations of CO2 in the air, completing the adsorption process. The saturated adsorbent is then sent to the desorption device. The desorbed adsorbent is then sent to the regeneration adsorbent delivery pipe, where it undergoes a cooling process at a higher temperature within a certain length of the pipe, regenerating the adsorbent and restoring its adsorption capacity. It then enters from the top of the adsorption device, and this cycle repeats, forming a continuous capture effect in the system.

[0023] The heat exchange fluid enters jacket two. Under the action of baffle two, the low-temperature fluid flows from low temperature to high temperature and then from high temperature to low temperature twice through the regeneration adsorbent delivery pipe. The heat is absorbed by the heat exchange fluid, and then it enters jacket one. Under the action of baffle one, it flows through jacket one twice from bottom to top and then from top to bottom. As the temperature of the desorption device rises, its heat is provided to the desorption device by the heat exchange fluid, thus realizing low-energy continuous carbon capture of air.

[0024] Compared with the prior art, the present invention has the following beneficial technical effects:

[0025] This invention proposes a low-energy-consumption continuous carbon capture system for air. It utilizes a dual-purpose adsorption unit fan, a jacketed connection between the desorption unit and the regenerated adsorbent delivery pipe, partial product gas heating and circulation in the desorption unit, and an integrated silo and adsorption unit. These measures reduce equipment energy consumption during adsorbent regeneration, temperature rise energy consumption during desorption, process energy consumption during adsorbent regeneration, and simplify the adsorption unit to reduce process energy consumption during adsorption. This achieves overall low-energy operation of a large-scale continuous carbon dioxide capture system for air. Furthermore, this application simply combines the adsorption unit, desorption unit, and adsorbent regeneration delivery pipeline, and integrates the silo and adsorption unit, easily achieving continuous carbon capture. It eliminates the need for an adsorbent silo, adsorbent regeneration unit, and associated valves, pumps, and other electrical and construction costs. The system has a simple structure and compact layout, demonstrating greater advantages in large-scale processing, higher application flexibility, reduced environmental impact, and is highly efficient, low-cost, and low-energy-consumption.

[0026] This invention also proposes a low-energy-consumption continuous carbon capture test system for air. The adsorbent enters the adsorption device and, under its own weight, accumulates and slowly descends. Simultaneously, air, driven by an induced draft fan, enters from around the adsorption device's cylinder, fully contacting the adsorbent. The active groups on the adsorbent capture low concentrations of CO2 from the air, completing the adsorption process. The saturated adsorbent is then sent to a desorption device. The desorbed adsorbent is then sent to a regeneration adsorbent delivery pipe. Within a certain length of the delivery pipe, the adsorbent undergoes a cooling process at a higher temperature, regenerating it and restoring its adsorption capacity. The regenerated adsorbent then enters from the top hopper section of the adsorption device. After gas-solid separation, excess gas is discharged, and the adsorbent accumulates in the hopper and slowly settles. This cycle continues, forming... The system achieves continuous carbon capture. The heat exchange fluid enters jacket two and, under the action of baffle two, flows from low to high temperature and then back to low temperature twice through the regeneration adsorbent delivery pipe. The heat is absorbed by the heat exchange fluid, and the fluid then enters jacket one. Under the action of baffle one, it flows from bottom to top and then from top to bottom twice. As the temperature of the desorption device rises, the heat is provided to the desorption device by the heat exchange fluid, avoiding heat loss from the desorption device. This achieves low-energy continuous carbon capture of air. The jacket not only satisfies heat self-sufficiency but also avoids heat loss from the desorption device. While compensating for the temperature difference between the high-temperature and low-temperature sections, it also provides excellent insulation, further reducing energy consumption during the adsorbent regeneration stage.

[0027] Furthermore, the hot gas outlet pipe is set as a straight pipe with a large diameter and irregular opening, so that the hot gas path is downward and first comes into thermal contact with the adsorbent at the bottom of the desorption device, and then the direction is changed from bottom to top to make thermal contact, so that the adsorbent at the bottom is desorbed first and regenerated first.

[0028] Furthermore, the desorption device is configured as a hot fluid jacket type, with the internal fluid medium being the field fluid medium. It is connected to the regeneration adsorbent delivery pipe, which is also configured as a jacket type. The purpose is to remove the heat from the higher-temperature adsorbent in the regeneration adsorbent delivery pipe. On the one hand, this reduces the temperature of the adsorbent after desorption, and on the other hand, it transfers the heat discarded to the desorption device. In particular, during the initial operation of the desorption device, it serves as supplementary heat, working together with the hot gas medium of the heater to maintain the desorption temperature after multiple cycles, thereby minimizing the heat consumption during the desorption stage.

[0029] Furthermore, without adding any additional material components to the system, this invention utilizes a portion of the product gas carbon dioxide, heated to approximately 80-100°C, the desorption temperature of the adsorbent, and sent from the hot gas outlet into the desorption device. This carries heat and exchanges heat with the saturated adsorbent, continuously circulating until the CO2 concentration of the product gas meets the requirements.

[0030] Furthermore, the method of using electrically heated carbon dioxide product gas to supplement heat in this invention can greatly reduce the energy consumption and water consumption of traditional steam-heated adsorbents, and avoid the loss of steam phase change heat and latent heat.

[0031] Furthermore, the high-temperature adsorbent needs to be cooled down. On the one hand, the regeneration process uses an induced draft fan to pneumatically transport room-temperature air through a regulating valve into the regenerated adsorbent transport pipeline, where it is fully mixed with the adsorbent and cooled down. On the other hand, low-quality circulating water is used on-site to connect the water in the jacket of the regenerated adsorbent transport pipeline with the water in the first jacket, and circulate them to cool down the adsorbent.

[0032] Furthermore, the adsorption unit's hopper section continuously receives regenerated adsorbent from the regenerated adsorbent delivery pipe, maintaining a near-full hopper state. Excess air from the regenerated adsorbent delivery pipe undergoes gas-solid separation at the top of the hopper section before being discharged through the hopper's exhaust port. The hopper acts as a buffer for the regenerated adsorbent and provides gas-solid separation during pneumatic conveying. The adsorbent in the hopper section slowly settles into the adsorption section of the adsorption unit, reacting fully with the incoming air. Saturated adsorbent, continuing to settle until it reaches the adsorption saturation section, is then sent to the next unit via the adsorbent outlet. This integrated design of the hopper and adsorption unit avoids the power consumption of the screw feeder between the hopper and adsorption unit, which is present in separate designs, and also avoids the power consumption of the cyclone separator required for direct pneumatic conveying of the adsorbent into the adsorption section. The hopper-based receiving and slow settling method significantly saves design space and further reduces energy consumption. Attached Figure Description

[0033] Figure 1 This is a schematic diagram of a low-energy-consumption continuous carbon capture test system for air according to the present invention;

[0034] Figure 2 This is a schematic diagram of the jacket of the continuous air carbon capture test system of the present invention;

[0035] Figure 3 This is a schematic diagram of the jacket 2 of the continuous air carbon capture test system of the present invention;

[0036] Figure 4 This is a schematic diagram of the adsorption device of the continuous carbon capture test system for air of the present invention.

[0037] In the diagram, 1-Adsorbent inlet, 2-Regenerated adsorbent conveying pipe, 3-Pneumatic conveying pipe, 4-Exhaust fan, 5-Regulating valve, 6-Adsorption device, 7-Adsorbent layer, 8-Adsorption device unloading valve, 9-Ball valve, 10-Hot gas outlet pipe, 11-Desorption device, 12-Heater, 13-Product gas CO2 outlet pipe, 14-Jacket 1, 15-Desorption device unloading valve, 16-Circulating water inlet, 17-Baffle 1, 18-Jacket 2, 19-Baffle 2, 20-Air outlet, 21-Hopper section, 22-Adsorption section, 23-Adsorption saturation section, 24-Hopper exhaust port, 25-Adsorbent outlet, 26-Gas-solid separation section. Detailed Implementation

[0038] The present invention will be further described in detail below with reference to specific embodiments. These descriptions are for explanation purposes only and are not intended to limit the scope of the invention.

[0039] To enable those skilled in the art to better understand the present invention, the technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort should fall within the scope of protection of the present invention.

[0040] A low-energy-consumption continuous carbon capture system for air and its operation method, such as Figure 1 As shown, it includes an equipment energy consumption system for reducing the adsorbent regeneration stage, a heating energy consumption system for reducing the adsorbent desorption stage, a process energy consumption system for reducing the adsorbent regeneration stage, and a process energy consumption system for simplifying the adsorption device to reduce the adsorption stage.

[0041] The energy consumption reduction system for the adsorbent regeneration stage includes an adsorption device 6, an induced draft fan 4, and a regulating valve.

[0042] Preferably, such as Figure 4 As shown, the adsorption device 6 has a cylindrical structure with a metal support for the cylinder. The inner and outer cylinders are metal mesh structures. The adsorbent is filled in the annular structure. Air passes through the adsorbent bed from all sides to capture carbon. Under the action of the induced draft fan, the air is discharged from the hollow part of the inner cylinder.

[0043] Preferably, the adsorption device 6 has a certain vertical length to ensure the discharge of pneumatically conveyed air and the passage of fresh air from all sides.

[0044] Preferably, the exhaust fan 4 has two functions: on the one hand, it serves as the air intake for the adsorption device 6;

[0045] Preferably, the induced draft fan 4 is a dual-purpose machine, controlled by a regulating valve, serving as a pneumatic conveying device for the regenerated adsorbent conveying pipe 2;

[0046] The method for reducing the energy consumption of heating during the desorption stage of the adsorbent includes an adsorption device discharge valve 8, a desorption device 11, a ball valve 9, a heater 12, and a hot gas outlet pipe 10.

[0047] Preferably, such as Figure 2 As shown, the desorption device 11 is a hot fluid jacket type, and the jacket 14 is divided into two sections by the partition 17. The inside of the jacket 14 is a heat exchange fluid, such as low-quality water.

[0048] Preferably, the desorption device 11 is provided with a product gas CO2 outlet 13 at the top;

[0049] Preferably, such as Figure 3 The regenerated adsorbent delivery pipe 2 shown is a jacketed type, and the jacket 2 18 is divided into two sections by the partition 2 19, which are connected to the jacket 1 14.

[0050] Preferably, a portion of the product gas passes through ball valve 9 and is heated to the adsorbent desorption temperature by heater 12, and is sent into the desorption device from the hot gas outlet to replenish the heat during the desorption process;

[0051] Preferably, the hot gas outlet 10 is a straight pipe with a large diameter and irregular opening, so that the hot gas path is downward and first comes into thermal contact with the adsorbent at the bottom of the desorption device 11, and then the direction is changed from bottom to top to make thermal contact, so that the adsorbent at the bottom is desorbed first and regenerated first.

[0052] The process energy consumption reduction of the adsorbent regeneration stage includes pneumatic conveying, a regenerated adsorbent conveying pipeline jacket, jacket one, jacket partition, and heat exchange fluid.

[0053] Preferably, the adsorbent regeneration temperature is achieved by using an induced draft fan to pneumatically transport and cool the adsorbent after passing through regulating valve 5;

[0054] Preferably, the adsorbent regeneration temperature is achieved by using a heat exchange fluid, such as low-quality circulating water on site, to connect the water in the jacket of the regenerated adsorbent delivery pipeline with the water in the first jacket for circulation.

[0055] Preferably, the heat exchange fluid enters the two zones divided by the partition from the bottom, and flows through the jacket twice, from bottom to top and then from top to bottom. The temperature of the pipe section decreases and the heat is absorbed by the heat exchange fluid.

[0056] Preferably, after the hot fluid absorbs heat, it enters the two zones divided by the partition 17 from the bottom, flows from bottom to top and then from top to bottom through the jacket 14, the temperature of the desorption device rises, and the heat is provided to the desorption device by the heat exchange medium to make up for the temperature difference between the high temperature section and the low temperature section, and to keep the desorption device warm.

[0057] like Figure 4 As shown, the simplified adsorption device reduces the process energy consumption of the adsorption stage by integrating the silo and the adsorption device into one unit. The adsorption device includes four parts: silo section 21, adsorption section 22, adsorption saturation section 23, and gas-solid separation section 26.

[0058] Furthermore, the adsorption device has a circular sleeve structure, with a material hopper section 21 at the top, an adsorption section 22 in the middle, and an adsorption saturation section 23 at the bottom. A certain amount of regenerated adsorbent slowly settles from the material hopper section to the annular gap of the adsorption device. The inner and outer walls of the adsorption section are perforated metal wire mesh structures, where the adsorbent reacts with the air. It continues to settle to the adsorption saturation section, which has a constricted structure, and the saturated adsorbent is sent to the desorption unit.

[0059] Furthermore, a hopper section 21 is provided at the upper end, and a hopper exhaust port 24 and a material receiving port are provided at the top of the hopper section 21. The air outlet 20 of the adsorption device is connected to the induced draft fan.

[0060] After the pneumatically conveyed regenerated adsorbent undergoes gas-solid separation in the gas-solid separation section, excess gas is discharged through the exhaust port, while the regenerated adsorbent continuously enters from the receiving port, where it is well buffered and accumulated in the silo section.

[0061] like Figure 1 The diagram shown is a schematic of a low-energy-consumption continuous carbon capture system for air according to the present invention. The adsorption device 6 is a cylindrical structure supported by a metal bracket. The adsorbent freely settles within the annular structure of the adsorption device, and air passes through the adsorbent bed from around the metal mesh. The adsorbent acts on the low-concentration carbon dioxide in the air, achieving the purpose of directly enriching and capturing carbon dioxide from the air.

[0062] This invention discloses a low-energy-consumption continuous carbon capture system for air, the working principle of which is as follows:

[0063] The adsorbent enters the annular space of the adsorption unit 6 from the adsorbent inlet 1. Under its own weight, the adsorbent moves downward through the annular space, accumulating and slowly descending. Simultaneously, air, driven by the induced draft fan 4, passes through the adsorbent layer 7 around the adsorption unit cylinder and makes full contact with it. The active groups on the adsorbent capture low concentrations of CO2 in the air. Under the action of the discharge valve 8, the slowly descending adsorbent completes the adsorption process and becomes saturated adsorbent, which is then sent to the desorption unit 11. Here, the saturated adsorbent completes the desorption process, and the desorbed carbon dioxide product gas is discharged from the CO2 outlet 13 at the top of the desorption unit and sent to the next unit for processing. A portion of the product gas acts as a heat medium, with its flow rate controlled by the ball valve 9. It is heated to the set temperature by the heater 12, passes through the hot gas outlet pipe 10, and is sent to the desorption unit to exchange heat with the saturated adsorbent. This cycle continues until the carbon dioxide concentration at the CO2 outlet 13 of the product gas meets the requirements, and the system reaches stable operation.

[0064] The desorbent after desorption is at a high temperature, such as 80℃. It is sent to the regenerated adsorbent conveying pipe 2 through the discharge valve 15 of the desorption device. In the conveying pipe of a certain length, the high-temperature adsorbent is cooled down, so that the adsorbent is regenerated and its adsorption capacity is restored. It enters from the top of the adsorption device and continues to cycle, forming a continuous capture effect of the system.

[0065] like Figure 1 This is a schematic diagram of a low-energy-consumption continuous carbon capture system for air. To further reduce the overall energy consumption of the system, four aspects are considered:

[0066] ① First, reduce the energy consumption of the equipment during the adsorbent regeneration stage. Configure the induced draft fan 4 of the adsorption unit for two purposes: firstly, to induced air flow into the adsorption unit; and secondly, to use a regulating valve 5 for pneumatic conveying of the regenerated adsorbent in the pneumatic conveying pipeline 3 of the regeneration adsorbent conveying pipe 2; based on an air handling capacity of 3600 Nm³. 3 The test system with a capacity of 2.88 kg / h can be adjusted from the original scheme of one 5.5 kW induced draft fan and one 4 kW pneumatic conveying fan to one 7.5 kW induced draft fan for dual use. If calculated according to the theoretical CO2 capture capacity of 2.88 kg / h, plus the estimated operating coefficient of the equipment, the system energy consumption can be reduced by 22-30%.

[0067] ② Further reduce the energy consumption of heating during the desorption stage of the adsorbent. The desorption device is configured as a hot fluid jacket type 14, with the internal fluid medium being on-site, such as low-quality circulating water. It is connected to the regeneration adsorbent delivery pipe 2, which is also configured as a jacket type. The purpose is to displace the heat of the higher-temperature adsorbent in the regeneration adsorbent delivery pipe. On the one hand, this lowers the temperature of the adsorbent after desorption, such as to 30°C, so that it can recover its regeneration capacity as much as possible in the delivery pipe. On the other hand, it transfers the heat of the discarded part to the desorption device, especially as supplementary heat for the desorption device during initial operation. It works together with the hot gas medium of the heater 12 to maintain the desorption temperature after multiple cycles of the desorption device, thereby minimizing the heat energy consumption during the desorption stage.

[0068] Further reduce the energy consumption for heating during the adsorbent desorption stage, such as... Figure 2 The diagram shows a schematic of the jacket of a low-energy-consumption continuous carbon capture test system for air. Without adding any additional material components to the system, a portion of the product gas carbon dioxide is heated to approximately 80-100°C, the desorption temperature of the adsorbent, and then fed into the desorption unit from the hot gas outlet. The large diameter of the hot gas outlet pipe and the asymmetrical structure of the pipe openings allow the hot gas to initially travel downwards, making thermal contact with the adsorbent at the bottom of the desorption unit, and then moving upwards for further thermal contact. The bottom adsorbent desorbs first and flows to the next regeneration unit, carrying heat and exchanging heat with the saturated adsorbent. This cycle continues until the CO2 concentration of the product gas meets the requirements, such as a concentration of 70% or higher. Using electrically heated carbon dioxide product gas to supplement the heat significantly reduces the energy and water consumption of traditional steam-heated adsorbent systems, avoiding the loss of steam phase change heat and latent heat.

[0069] ③ Further reduce the energy consumption during the adsorbent regeneration stage. For example... Figure 3The diagram shows a schematic of jacket two in a low-energy-consumption continuous carbon capture test system for air. The high-temperature adsorbent needs to be cooled from its desorption temperature of 80°C to its adsorption temperature of 30°C. On one hand, the regeneration process utilizes an induced draft fan, which, after regulating valves, pneumatically transports room-temperature air into the regeneration adsorbent delivery pipeline, where it is thoroughly mixed with the adsorbent and cooled. On the other hand, low-quality circulating water is used to connect the water in jacket two (18) of the regeneration adsorbent delivery pipeline with the water in jacket one, creating a circulating flow. The heat exchange fluid, such as circulating water, enters jacket two (18) from the circulating water inlet 16. Under the action of baffle two (19), the low-temperature circulating water is cooled by the valve pressure difference. The fluid flows through the regenerated adsorbent delivery pipe twice, from high temperature to low temperature and from bottom right to top and from top right to bottom. As the temperature of the pipe section decreases, the heat is absorbed by the heat exchange fluid and enters the jacket 14. Under the action of the baffle 17, it flows through the jacket from bottom to top and then from top to bottom. As the temperature of the desorption device increases, the heat is provided to the desorption device by the heat exchange medium. The jacket not only meets the self-sufficiency of heat but also avoids the heat loss of the desorption device. While compensating for the temperature difference between the high-temperature and low-temperature sections, it also plays a good role in heat preservation, further reducing the energy consumption of the adsorbent regeneration stage.

[0070] ④ Simplify the adsorption device to reduce the energy consumption of the adsorption stage. For example... Figure 4 The diagram shows the segmented structure of the adsorption device in the continuous carbon capture test system of the present invention. The adsorption device 6 is divided into four parts: a hopper section 21, an adsorption section 22, an adsorption saturation section 23, and a gas-solid separation section 26. The hopper section 21 continuously receives regenerated adsorbent from the regenerated adsorbent delivery pipe 2, maintaining a normal state where the hopper is almost full. Excess air from the regenerated adsorbent delivery pipe 3 is separated into gas and solid by the gas-solid separation section 26 at the top of the hopper section and discharged through the hopper exhaust port 24. The hopper serves as a buffer for the regenerated adsorbent and a gas-solid separation function for pneumatic conveying. The adsorbent in the hopper section slowly settles into the adsorption section 22 of the adsorption device 6, where it reacts fully with the air entering from the surrounding area and is adsorbed. The saturated adsorbent that continues to settle into the adsorption saturation section 23 is sent to the next unit through the adsorbent outlet 25. The integrated design of the silo and the adsorption unit avoids the power consumption of the screw feeder between the silo and the adsorption unit when they are designed separately, and avoids the power consumption of the cyclone separator in the design of directly conveying the adsorbent into the adsorption section by pneumatic conveying. The method of receiving the material in the silo and slowly settling it into the adsorption section greatly saves design space and further reduces energy consumption.

[0071] It should be noted that the terms "a," "b," etc., in the specification, claims, and accompanying drawings of this invention are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence. It should be understood that such data can be interchanged where appropriate so that embodiments of the invention described herein can be implemented in orders other than those illustrated or described herein. When a component is referred to as being "fixed to" another component, it can be directly on the other component or there may be an intervening component. When a component is considered to be "connected to" another component, it can be directly connected to the other component or there may be an intervening component. When a component is considered to be "disposed on" another component, it can be directly disposed on the other component or there may be an intervening component.

[0072] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. The terminology used herein in the specification of this invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.

[0073] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any way. Those skilled in the art can readily implement the present invention based on the accompanying drawings and the above description. However, any modifications, alterations, or variations made by those skilled in the art without departing from the scope of the present invention, utilizing the disclosed technical content, are equivalent embodiments of the present invention. Furthermore, any modifications, alterations, or variations made to the above embodiments based on the essential technology of the present invention are still within the protection scope of the present invention.

Claims

1. A low-energy-consumption continuous carbon capture system for air, characterized in that, include, Equipment energy consumption system, heating energy consumption system and process energy consumption system; The energy consumption system of the equipment includes an adsorption device (6) and an induced draft fan (4), wherein the air outlet of the adsorption device (6) is connected to the inlet of the induced draft fan (4). The heating energy consumption system includes a desorption device (11), which is a hot fluid jacket type. A jacket (14) is provided on the outer wall of the desorption device (11). The top and bottom of the jacket (14) are separated by a partition (17). The interior of the jacket (14) is a heat exchange fluid. The adsorbent inlet of the desorption device (11) is connected to the adsorbent outlet of the adsorption device (6). The process energy consumption system includes a regenerated adsorbent delivery pipe (2) and a pneumatic delivery pipe (3). The adsorbent outlet of the desorption device (11) is connected to one end of the regenerated adsorbent delivery pipe (2), and the other end of the regenerated adsorbent delivery pipe (2) is connected to the adsorption device (6). The regenerated adsorbent delivery pipe (2) is a jacketed type. A second jacket (18) is provided on the outside of the regenerated adsorbent delivery pipe (2). The second jacket (18) is separated radially by a second partition (19). One outlet of the blower (4) is connected to the pneumatic delivery pipe (3). The adsorption device (6) includes, from top to bottom, a hopper section (21), an adsorption section (22), and an adsorption saturation section (23). A gas-solid separation section (26) is provided on the top of one side of the hopper section (21). The inlet of the hopper section (21) is connected to the regenerated adsorbent conveying pipe (2). The adsorption saturation section (23) is connected to the adsorbent inlet of the desorption device (11). The outlet of the gas-solid separation section (26) is connected to the hopper exhaust port (24). The heating energy consumption system also includes a heater (12); the top of the desorption device is provided with a product gas CO2 outlet pipe (13), a branch of the product gas CO2 outlet pipe (13) is connected to the inlet of the heater (12), and the outlet of the heater (12) is connected to the desorption device (11) through a hot gas outlet pipe (10) to form a circulation loop.

2. The low-energy-consumption continuous carbon capture system for air according to claim 1, characterized in that, The adsorption device (6) is a cylindrical structure and is supported by a metal bracket; the inner and outer walls of the adsorption section (22) are metal mesh annular gap structures, and the adsorbent is filled in the annular gap structure to form an adsorbent layer (7).

3. The low-energy-consumption continuous carbon capture system for air according to claim 1, characterized in that, A ball valve (9) is provided at the inlet of the heater (12).

4. The low-energy-consumption continuous carbon capture system for air according to claim 1, characterized in that, The heat exchange fluid is water.

5. The low-energy-consumption continuous carbon capture system for air according to claim 1, characterized in that, A regulating valve (5) is installed on the pipeline between the outlet of the induced draft fan (4) and the pneumatic conveying pipeline (3).

6. The low-energy-consumption continuous carbon capture system for air according to claim 1, characterized in that, The adsorption device (6) is equipped with an adsorbent discharge valve (8) at the adsorbent outlet.

7. The low-energy-consumption continuous carbon capture system for air according to claim 1, characterized in that, The outlet of the induced draft fan (4) is connected to the outside air.

8. A method for operating a low-energy-consumption continuous carbon capture air test system, based on the low-energy-consumption continuous carbon capture air test system according to any one of claims 1-7, characterized in that, include, The adsorbent enters the adsorption device (6) and accumulates and slowly descends under its own weight. At the same time, air enters from the cylinder of the adsorption device (6) under the action of the induced draft fan (4) and comes into full contact with the adsorbent. The active groups on the adsorbent capture the low concentration of CO2 in the air. The adsorbent completes the adsorption process and becomes a saturated adsorbent, which is then sent to the desorption device (11). The desorbed adsorbent is sent to the regeneration adsorbent delivery pipe (2). In the regeneration adsorbent delivery pipe (2), the adsorbent is cooled down, which regenerates the adsorbent and restores its adsorption capacity. It enters from the top of the adsorption device (6) and repeats this cycle to form a continuous capture effect of the system. The heat exchange fluid enters the second jacket (18). Under the action of the second partition (19), the low-temperature fluid flows from low temperature to high temperature and then from high temperature to low temperature under the action of pressure difference. The heat is absorbed by the heat exchange fluid in the regeneration adsorbent delivery pipe (2) twice, and then enters the first jacket (14). Under the action of the first partition (17), it flows through the first jacket (14) twice from bottom to top and then from top to bottom. As the temperature of the desorption device (11) rises, its heat is provided to the desorption device (11) by the heat exchange fluid, thereby realizing low-energy continuous carbon capture of air.

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