A low energy regenerated three-bed radial flow adsorber and method of use

Abstract

The application discloses a kind of low-energy consumption regenerated three-layer radial flow adsorbers and use method, the adsorber includes tank body and coaxially arranged multilayer cylindrical screen assembly, between which is formed by sequentially arranged from outside to inside external adsorption layer, middle adsorption layer and internal adsorption layer;External adsorption layer fills low-temperature desorption material, middle adsorption layer fills active alumina, internal adsorption layer fills molecular sieve, and the regeneration temperature of three is sequentially increased.Adsorption, raw gas flows through each layer from outside to inside, and removes water and carbon dioxide in stages;When regenerating, high-temperature gas flows from inside to outside, and the temperature gradually decreases, sequentially matches the regeneration needs of molecular sieve, active alumina and low-temperature desorption material, and realizes heat energy cascade utilization.Compared with traditional structure, the adsorber of the application shortens 39.6% of annual heat blowing operation time, and the desorption energy consumption is significantly reduced, with the advantages of efficient adsorption and low-energy consumption regeneration.

Description

Technical Field

[0001] This invention relates to the fields of gas separation and liquid air energy storage technology, and in particular to a low-energy-consumption regenerative three-layer radial flow adsorber and its usage method. Background Technology

[0002] In gas separation and related industrial applications, feed gases typically contain a certain amount of moisture and impurities such as carbon dioxide. These impurities are prone to condensation or freezing under low-temperature or high-pressure conditions during system operation, which not only reduces system efficiency but can also cause flow channel blockage, equipment damage, and operational safety hazards. Therefore, before the gas enters subsequent compression, cooling, or storage units, it usually needs to undergo thorough purification to remove moisture and carbon dioxide.

[0003] Existing gas purification devices mostly employ axial flow adsorption beds or radial flow adsorption structures. Among them, axial flow adsorption beds have problems such as large bed pressure drop, uneven gas distribution, and low utilization rate of adsorption materials. Radial flow adsorption structures improve gas distribution and pressure drop to some extent, but they are mostly single-layer or double-layer structures, and still have shortcomings such as concentrated adsorption load and high desorption energy consumption under high water content or high carbon dioxide conditions.

[0004] In recent years, to improve the processing capacity and flow field uniformity of adsorbers, radial flow adsorbers with multi-layer screen designs have emerged. These adsorbers form inner and outer adsorption layers by using multiple cylindrical screens and employ a counter-current flow path of adsorption from the outside in and regeneration from the inside out, thus improving the uniformity of gas distribution to some extent. However, in actual operation, to maintain the regeneration effect of the outer adsorbent material and ensure sufficient desorption of adsorbates from the adsorbent surface, the regeneration process still requires continuous introduction of high-temperature gas to ensure that the outer layer reaches the required regeneration temperature. For example... Figure 1 As shown, in the regeneration process of traditional adsorbers, a large amount of heat is discharged with the regeneration gas and is not effectively utilized, resulting in significant energy waste.

[0005] Therefore, in pursuit of high system efficiency, energy saving and long-term stable operation, there is a need for a gas adsorber with a reasonable structure, scientific adsorption layer configuration and low energy consumption regeneration characteristics. Summary of the Invention

[0006] To address the problems of low utilization rate of adsorbent materials and high desorption energy consumption in existing gas adsorption purification devices, the present invention aims to provide a low-energy-consumption regeneration three-layer radial flow adsorber and its adsorption and desorption method. This adsorber consists of three adsorption layers arranged radially from the outside to the inside, with progressively increasing regeneration temperature requirements: an outer low-temperature desorption material, a middle activated alumina layer, and an inner molecular sieve. It employs a counter-current flow path, with adsorption from the outside in and regeneration from the inside out. In the adsorption stage, the raw gas sequentially passes through the three layers to remove moisture and carbon dioxide, improving the utilization rate of the adsorbent materials. In the desorption stage, the high-temperature regeneration gas flows from the inside to the outside, with its heat progressively matching the regeneration needs of each layer, achieving tiered energy utilization and significantly reducing regeneration energy consumption.

[0007] To achieve the above-mentioned objectives, the present invention adopts the following technical solution:

[0008] A low-energy-consumption regenerative three-layer radial flow adsorber, comprising:

[0009] Tank body;

[0010] A multi-layer cylindrical screen assembly is coaxially disposed inside the tank, and the lower end of the multi-layer cylindrical screen assembly is fixedly connected to a head disposed inside the tank.

[0011] The multi-layer cylindrical screen assembly forms an outer adsorption layer, a middle adsorption layer, and an inner adsorption layer arranged radially from the outside to the inside. The outer adsorption layer is filled with an adsorption material with low-temperature desorption properties, the middle adsorption layer is filled with activated alumina, and the inner adsorption layer is filled with molecular sieves. The regeneration temperature of the outer adsorption layer, the middle adsorption layer, and the inner adsorption layer increases sequentially.

[0012] The adsorber is also provided with an adsorption flow path and a regeneration flow path. Specifically, the adsorption flow path is as follows: the raw material gas flows from the outside to the inside through the outer adsorption layer, the middle adsorption layer and the inner adsorption layer in sequence.

[0013] The regeneration flow path is specifically as follows: high-temperature regeneration gas flows from the inside to the outside through the inner adsorption layer, the middle adsorption layer and the outer adsorption layer in sequence. The temperature of the high-temperature regeneration gas gradually decreases during the flow process, matching the regeneration temperature requirements of the inner adsorption layer, the middle adsorption layer and the outer adsorption layer in sequence.

[0014] Preferably, the lower part of the tank is provided with an adsorption inlet pipe and a desorption inlet pipe with a coaxial sleeve structure. The desorption inlet pipe is located inside the adsorption inlet pipe and extends into the interior of the tank, and is used to directly introduce high-temperature regeneration gas into the area where the internal adsorption layer is located.

[0015] The upper part of the tank is equipped with an adsorption outlet pipe.

[0016] Preferably, a heat insulation structure is provided on the outside of the desorption air intake pipe.

[0017] Preferably, the top of the tank is provided with a first inlet, a second inlet and a third inlet, which correspond to the outer adsorption layer, the middle adsorption layer and the inner adsorption layer respectively, and are used to independently fill or replenish the corresponding adsorption material to each adsorption layer.

[0018] Preferably, the outer adsorption layer is defined by an outer cylindrical screen and a first middle cylindrical screen; the middle adsorption layer is defined by a first middle cylindrical screen and a second middle cylindrical screen; and the inner adsorption layer is defined by a second middle cylindrical screen and an inner cylindrical screen.

[0019] This invention also provides a method for using a low-energy-consumption regenerable three-layer radial flow adsorber, including an adsorption stage and a desorption stage, the specific steps of which are as follows:

[0020] Adsorption stage: The ambient temperature raw gas enters the adsorber through the adsorption inlet pipe and flows radially through the outer adsorption layer first. A large amount of water in the gas is adsorbed by the adsorption material with low-temperature desorption performance. Then the gas enters the middle adsorption layer, where the gas treated by the outer adsorption layer is deeply dehydrated. Finally, the gas flows through the molecular sieve of the inner adsorption layer to adsorb carbon dioxide in the gas. The purified gas is discharged through the adsorption outlet pipe.

[0021] Desorption stage: High-temperature regeneration gas enters the adsorber through the desorption inlet pipe and first flows radially through the inner adsorption layer, where the carbon dioxide adsorbed in the molecular sieve is desorbed under high temperature conditions. Subsequently, the temperature of the regeneration gas gradually decreases and continues to flow through the middle adsorption layer, causing the moisture adsorbed in the activated alumina to be released. Finally, the regeneration gas with a further reduced temperature flows through the outer adsorption layer, using the remaining heat to complete the desorption of moisture in the adsorption material with low-temperature desorption performance. After the hot blowing is completed, the supply of high-temperature regeneration gas is stopped, and then cold blowing gas is introduced to cool the adsorption layer. The cold blowing gas flows through each adsorption layer in the same flow direction as the hot blowing. Both the hot blowing desorption gas and the cold blowing gas are discharged through the adsorption inlet pipe.

[0022] Preferably, during the desorption stage, the inlet temperature of the high-temperature regeneration gas is 180-220°C, the temperature drops to 140-160°C after flowing through the inner adsorption layer, the temperature drops to 100-120°C after flowing through the middle adsorption layer, and the temperature drops to below 80°C after flowing through the outer adsorption layer.

[0023] Compared with the prior art, the present invention has at least the following beneficial effects:

[0024] 1. This invention, through the synergistic design of a regeneration temperature gradient of three layers of materials and a reverse regeneration flow path, enables the tiered utilization of heat from the high-temperature regeneration gas—the high-temperature section is used to regenerate molecular sieves, the medium-temperature section is used to regenerate activated alumina, and the low-temperature section utilizes residual heat to regenerate the outer layer material. For example... Figure 3 and Figure 4 The comparison shows that, under the same hot blowing time, the bed moisture content of the three-layer structure of the present invention decreases significantly faster than that of the traditional two-layer structure; even under shorter hot blowing conditions, the three-layer structure can achieve the regeneration effect that the two-layer structure requires a longer hot blowing time to achieve. This means that the present invention can significantly shorten the hot blowing time while ensuring the regeneration effect, thereby reducing regeneration energy consumption. As shown in Table 1, the annual hot blowing operation time is shortened from 1200h to 724.8h, and the additional heat removal energy consumption is reduced by 39.6%;

[0025] 2. The outer adsorption layer uses an adsorbent material with low-temperature desorption properties, requiring a regeneration temperature far lower than that of molecular sieves and activated alumina. This design not only allows the outer layer material to effectively utilize the residual heat from the regeneration of the first two layers to complete desorption, but also reduces the overall regeneration process's dependence on high-temperature heat sources. Compared to traditional structures where all adsorbent materials require high-temperature regeneration, the low-temperature layer design of this invention further reduces regeneration energy consumption and extends the equipment's service life.

[0026] 3. During the desorption process, the low-to-medium grade waste heat generated by the system operation can be used as a regenerated heat source, reducing the dependence on high-temperature heating equipment. This feature makes the present invention not only suitable for new installations, but also easy to integrate into existing industrial systems. By recovering waste heat, the overall energy utilization efficiency can be improved, which has good economic benefits and promotional value. Attached Figure Description

[0027] Figure 1 The outlet temperature change curve of a traditional double-layer adsorber during the desorption process;

[0028] Figure 2 This is a schematic diagram of the structure of the three-layer radial flow adsorber according to Embodiment 1 of the present invention;

[0029] Figure 3 This is a curve showing the change in bed moisture content over time during desorption of a two-layer radial flow adsorber under different combinations of hot and cold blowing times, as described in Embodiment 2 of the present invention.

[0030] Figure 4 The curves showing the change of bed moisture content over time during desorption of the three-layer radial flow adsorber in Embodiment 2 of the present invention under different combinations of hot and cold blowing times are shown.

[0031] Figure 5 This is a comparison chart of the hot blowing time of two-layer and three-layer radial flow adsorbers under different moisture contents in Example 2 of the present invention;

[0032] Wherein, 1-Adsorption inlet pipe; 2-Tank body; 3-End cap; 4-Outer cylindrical screen; 5-First middle cylindrical screen; 6-Second middle cylindrical screen; 7-Inner cylindrical screen; 8-Outer adsorption layer; 9-Middle adsorption layer; 10-Inner adsorption layer; 11-First feed inlet; 12-Second feed inlet; 13-Third feed inlet; 14-Adsorption outlet pipe; 15-Desorption inlet pipe. Detailed Implementation

[0033] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings, so that those skilled in the art can better understand the advantages and features of the present invention, thereby making a clearer definition of the scope of protection of the present invention. The embodiments described in this invention are only some embodiments of the present invention, not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are within the scope of protection of the present invention.

[0034] It should be noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the exemplary embodiments according to this application. As used herein, the singular form is intended to include the plural form as well, unless the context clearly indicates otherwise. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0035] This invention provides a low-energy-consumption regenerable three-layer radial flow adsorber, which is a radial flow adsorber for gas purification with low-energy-consumption regeneration characteristics. It achieves the stepwise adsorption and removal of moisture and carbon dioxide in the gas by setting three adsorption layers with different functions in the radial direction in the same adsorber and using radial flow. This improves the overall utilization efficiency of the adsorption material and reduces the energy consumption in the desorption process, ultimately achieving efficient and stable removal of water and carbon dioxide from the gas.

[0036] In the implementation of this invention, such as Figure 2 As shown, a low-energy-consumption regeneration three-layer radial flow adsorber specifically includes: an adsorption inlet pipe 1, a tank 2, a head 3, an outer cylindrical screen 4, a first middle cylindrical screen 5, a second middle cylindrical screen 6, an inner cylindrical screen 7, an outer adsorption layer 8, a middle adsorption layer 9, an inner adsorption layer 10, a first feed inlet 11, a second feed inlet 12, a third feed inlet 13, an adsorption outlet pipe 14, and a desorption inlet pipe 15.

[0037] The tank body 2 is a vertical cylindrical structure. The lower part of the tank body 2 is connected to the adsorption inlet pipe 1 and the desorption inlet pipe 15, and the upper part of the tank body 2 is connected to the adsorption outlet pipe 14. The desorption inlet pipe 15 is coaxially arranged with the adsorption inlet pipe 1 and is a sleeve structure. The desorption inlet pipe 15 is inside the adsorption inlet pipe 1 and extends into the interior of the tank body 2, and is used to directly introduce the high-temperature regeneration gas into the area where the internal adsorption layer 10 is located.

[0038] The desorption inlet pipe 15 is equipped with an insulation structure on the outside to reduce heat loss of the regenerated gas during transportation.

[0039] The lower ends of the outer cylindrical screen 4, the first middle cylindrical screen 5, the second middle cylindrical screen 6, and the inner cylindrical screen 7 are all fixedly connected to the end cap 3.

[0040] An outer adsorption layer 8 is formed between the outer cylindrical screen 4 and the first middle cylindrical screen 5, and the outer adsorption layer 8 is filled with an adsorption material with low-temperature desorption properties.

[0041] A central adsorption layer 9 is formed between the first central cylindrical screen 5 and the second central cylindrical screen 6, and the central adsorption layer 9 is filled with activated alumina adsorption material.

[0042] An internal adsorption layer 10 is formed between the second central cylindrical screen 6 and the inner cylindrical screen 7, and the inner adsorption layer 10 is filled with molecular sieve adsorption material.

[0043] The tank body 2 is provided with a first inlet 11, a second inlet 12 and a third inlet 13 at the top. The inlets correspond to the outer adsorption layer 8, the middle adsorption layer 9 and the inner adsorption layer 10 respectively, and are used to independently fill or replenish the corresponding adsorption material to each adsorption layer to achieve independent maintenance of each layer.

[0044] The regeneration temperature requirements of the three adsorption materials mentioned above increase sequentially: molecular sieves require a higher regeneration temperature (typically 150-200℃) to achieve deep CO2 desorption; activated alumina requires a lower regeneration temperature (typically 100-150℃); while the low-temperature desorption material used in the external adsorption layer can complete water desorption at a lower temperature of 80-100℃. This temperature gradient lays the foundation for subsequent energy cascade utilization.

[0045] Example 2

[0046] This embodiment describes the working process of a low-energy-consumption regeneration three-layer radial flow adsorber, specifically the adsorption stage and the desorption stage.

[0047] Adsorption stage: The raw gas containing CO2 and H2O enters the tank 2 through the adsorption inlet pipe 1 at 20℃, flows radially from the outside to the inside through each adsorption layer, and is discharged through the adsorption outlet pipe 14. During this process, most of the moisture is first removed by the low-temperature desorption material in the outer adsorption layer 8, then further dehydrated by the activated alumina in the middle adsorption layer 9, and finally CO2 in the gas is adsorbed by the molecular sieve in the inner adsorption layer 10 until the CO2 concentration in the purified gas reaches 1 ppm, at which point the adsorption ends. The three layers of adsorption materials have clearly defined functions, avoiding the problem of concentrated load on a single material and improving adsorption efficiency.

[0048] Desorption stage: 200℃ regeneration gas enters the adsorber through desorption inlet pipe 15 and first flows radially through the inner adsorption layer 10. At this time, the gas temperature is about 200℃, which meets the high temperature conditions required for molecular sieve regeneration, promoting the full desorption of carbon dioxide adsorbed in the molecular sieve. Subsequently, after releasing heat, the temperature of the regeneration gas gradually decreases to about 160℃ and continues to flow through the middle adsorption layer 9. At this time, the gas temperature is still within the temperature range required for the regeneration of activated alumina, causing the moisture adsorbed in the activated alumina to be released. Finally, the regeneration gas with a further reduced temperature flows through the outer adsorption layer 8. Although the gas temperature has dropped below 100℃ at this time, it fully matches the regeneration temperature requirements of the external low-temperature desorption material. The remaining heat can be used to complete the desorption of moisture in the adsorption material with low-temperature desorption performance.

[0049] Through the above process, the heat of the high-temperature regeneration gas is utilized in stages: the high-temperature stage is used to regenerate the molecular sieve, the medium-temperature stage is used to regenerate the activated alumina, and the low-temperature stage is used to regenerate the external low-temperature desorption material. This "temperature-material" matching design allows the thermal energy of the regeneration gas to be fully utilized step by step, achieving complete regeneration of each adsorption layer without the need for continuous high-temperature gas supply.

[0050] Cold blowing stage: After hot blowing, the high-temperature regeneration gas is stopped, and then room-temperature gas at 20°C (cold blowing gas) is introduced, flowing from the inside to the outside through each adsorption layer along the same path as hot blowing. The purpose of cold blowing is twofold: first, to lower the temperature of each adsorption layer to near the adsorption operating temperature, allowing the adsorbent material to regain its adsorption capacity; and second, to thoroughly purge any remaining desorbed gas from the adsorber. When the temperature of the adsorption layer drops to near the adsorption operating temperature and meets the requirements for re-entering the adsorption operating condition, the cold blowing process ends, and the adsorber enters the next adsorption cycle. Both the hot blowing desorbed gas and the cold blowing gas are discharged through adsorption inlet pipe 1.

[0051] To further illustrate the performance advantages of the three-layer radial flow adsorption structure of this invention in the desorption process, simulation analyses were conducted on the desorption processes of two-layer and three-layer radial flow adsorption beds under different combinations of hot and cold blowing times. The results are as follows: Figure 3 and Figure 4 As shown.

[0052] In this invention, the two-layer radial flow adsorption bed uses activated alumina and molecular sieves as adsorption materials. The three-layer radial flow adsorption bed of this invention adds an outer adsorption layer filled with an adsorption material with low-temperature desorption performance on the outside, thereby forming a three-layer radial flow structure in which the outer adsorption layer, the middle adsorption layer and the inner adsorption layer are arranged in sequence.

[0053] In this embodiment, the two-layer radial flow adsorption bed is filled with 1016.3 kg of 13X molecular sieve and 508.9 kg of activated alumina; the three-layer radial flow adsorption bed is filled with 1016.3 kg of 13X molecular sieve, 316.1 kg of activated alumina, and 192.8 kg of low-temperature desorption material.

[0054] In this embodiment, the initial water volume for the desorption process is 1844 mol. The initial water volume refers to the total amount of water adsorbed in the adsorption bed after 4 hours of continuous adsorption of saturated humid air at a mass flow rate of 1.714 kg / s at 17°C. Figure 3 , Figure 4 and Figure 5 The analysis of the desorption process in the data is based on this initial water volume condition.

[0055] like Figure 3 As shown, in a two-layer radial flow adsorption bed, the overall moisture content of the bed gradually decreases over time as the desorption process proceeds. When the hot blowing time is short and the cold blowing time is long, the bed still has a certain residual moisture content in the later stage of desorption, indicating that under conventional desorption conditions, some moisture is difficult to be fully desorbed in a short time.

[0056] like Figure 4 As shown, when using the three-layer radial flow adsorption bed of the present invention, under the same or similar combinations of hot and cold blowing times, the rate of decrease in bed moisture content is significantly accelerated, and a low residual moisture content level can be maintained in the later stage of desorption. Even under the condition of relatively short hot blowing time, the three-layer radial flow adsorption bed can still achieve a relatively sufficient moisture desorption effect. This indicates that the three-layer structure can achieve more complete desorption in a shorter hot blowing time, and the outer low-temperature material effectively utilizes the residual heat after the regeneration of the first two layers.

[0057] contrast Figure 3 and Figure 4 It can be seen that, compared with the traditional two-layer radial flow adsorption bed, the three-layer radial flow adsorption bed of the present invention exhibits superior desorption kinetic characteristics in the desorption stage, mainly manifested in: (1) within the same hot blowing time, the water content of the three-layer structure bed decreases faster, and the desorption rate is significantly improved; (2) under the condition of relatively short hot blowing time, the three-layer radial flow adsorption bed can still achieve a relatively sufficient water desorption effect, reducing the sensitivity to hot blowing time; (3) from Figure 5It can be seen that, under the same moisture content, the hot blowing time required by the three-layer radial flow adsorber of the present invention is generally lower than that of the traditional two-layer structure. The three-layer structure can reduce the hot blowing time by about 35% to 40%. This effect is mainly attributed to the synergistic matching of the regeneration temperature gradient of the three-layer material and the temperature drop gradient of the regeneration gas flow: the outer low-temperature desorption material can effectively utilize the residual heat after the regeneration of the first two layers to complete the desorption, thereby improving the overall desorption efficiency and reducing the regeneration energy consumption.

[0058] Table 1. Economic analysis of different adsorber hot-blowing regeneration processes

[0059] This adsorbent Traditional double-layer adsorbent Industrial electricity price (RMB / kWh) 0.81 0.81 Hot air blowing operation time (h / year) 724.8 1200 <![CDATA[High-temperature regeneration air volume per hour (m 3 / h)]]> 1870.3 1870.3 Electric heating power (kW) 113.26 113.26 Desorption process heating energy consumption (kWh / year) 82090.8 135912 Excluding the additional heat purchase electricity price (ten thousand yuan / year) 8.21 13.59

[0060] As shown in Table 1, the optimized adsorption layer structure of this invention reduces the annual hot blowing operation time from 1200 hours to 724.8 hours, resulting in a 39.6% reduction in annual heat removal energy consumption. Based on an industrial electricity price of RMB 0.81 / kWh, the annual cost of electricity for heat removal is reduced from RMB 135,900 to RMB 82,100, resulting in annual electricity savings of approximately RMB 53,800. Therefore, under long-term operating conditions, the adsorber of this invention demonstrates excellent economic efficiency in reducing regeneration energy consumption and operating costs.

[0061] In summary, this invention achieves tiered utilization of regeneration heat energy through the temperature gradient design of the three-layer adsorption material and the synergy of the reverse regeneration flow path. While ensuring adsorption performance, it significantly reduces regeneration energy consumption (by up to 39.6%), providing a technical solution with both high efficiency and energy saving characteristics for the field of gas purification.

Claims

1. A low-energy-consumption regenerative three-layer radial flow adsorber, characterized in that, include: Tank body (2); A multi-layer cylindrical screen assembly is coaxially disposed inside the tank body (2), and the lower end of the multi-layer cylindrical screen assembly is fixedly connected to the end cap (3) disposed inside the tank body (2). Among them, the multi-layer cylindrical screen assembly forms an outer adsorption layer (8), a middle adsorption layer (9), and an inner adsorption layer (10) arranged radially from the outside to the inside. The outer adsorption layer (8) is filled with an adsorption material with low-temperature desorption performance, the middle adsorption layer (9) is filled with activated alumina, and the inner adsorption layer (10) is filled with molecular sieve. The regeneration temperature of the outer adsorption layer (8), the middle adsorption layer (9), and the inner adsorption layer (10) increases sequentially. The adsorber is also provided with an adsorption flow path and a regeneration flow path. The adsorption flow path is specifically as follows: the raw material gas flows from the outside to the inside through the outer adsorption layer (8), the middle adsorption layer (9) and the inner adsorption layer (10). The regeneration flow path is as follows: the high-temperature regeneration gas flows from the inside to the outside through the inner adsorption layer (10), the middle adsorption layer (9) and the outer adsorption layer (8). The temperature of the high-temperature regeneration gas gradually decreases during the flow process, which is matched with the regeneration temperature requirements of the inner adsorption layer (10), the middle adsorption layer (9) and the outer adsorption layer (8) in sequence.

2. The low-energy-consumption regenerative three-layer radial flow adsorber according to claim 1, characterized in that, The lower part of the tank (2) is provided with an adsorption inlet pipe (1) and a desorption inlet pipe (15) with a coaxial sleeve structure. The desorption inlet pipe (15) is located inside the adsorption inlet pipe (1) and extends into the tank (2) to directly introduce high-temperature regeneration gas into the area where the internal adsorption layer (10) is located. The upper part of the tank (2) is provided with an adsorption outlet pipe (14).

3. The low-energy-consumption regenerative three-layer radial flow adsorber according to claim 1, characterized in that, The outer side of the desorption air inlet pipe (15) is provided with a heat insulation structure.

4. The low-energy-consumption regenerative three-layer radial flow adsorber according to claim 1, characterized in that, The top of the tank (2) is provided with a first inlet (11), a second inlet (12) and a third inlet (13), which correspond to the outer adsorption layer (8), the middle adsorption layer (9) and the inner adsorption layer (10) respectively, and are used to independently fill or supplement the corresponding adsorption material to each adsorption layer.

5. The low-energy-consumption regenerative three-layer radial flow adsorber according to claim 1, characterized in that, The outer adsorption layer (8) is defined by an outer cylindrical screen (4) and a first middle cylindrical screen (5); the middle adsorption layer (9) is defined by a first middle cylindrical screen (5) and a second middle cylindrical screen (6); the inner adsorption layer (10) is defined by a second middle cylindrical screen (6) and an inner cylindrical screen (7).

6. A method of using a three-layer radial flow adsorber with low energy consumption regeneration according to any one of claims 1 to 5, characterized in that, It includes an adsorption stage and a desorption stage, and the specific steps are as follows: Adsorption stage: The ambient temperature raw gas enters the adsorber through the adsorption inlet pipe (1) and flows through the outer adsorption layer (8) in the radial direction. A large amount of water in the gas is adsorbed by the adsorption material with low temperature desorption performance. Then the gas enters the middle adsorption layer (9) to deeply remove water from the gas after it has been treated by the outer adsorption layer. Finally, the gas flows through the inner adsorption layer (10) and the molecular sieve adsorbs carbon dioxide in the gas. The purified gas is discharged through the adsorption outlet pipe (14). Desorption stage: High-temperature regeneration gas enters the adsorber through the desorption inlet pipe (15) and first flows through the inner adsorption layer (10) in the radial direction, causing the carbon dioxide adsorbed in the molecular sieve to desorb under higher temperature conditions; then the temperature of the regeneration gas gradually decreases and continues to flow through the middle adsorption layer (9), causing the water adsorbed in the activated alumina to be released; finally, the regeneration gas with a further reduced temperature flows through the outer adsorption layer (8), using the remaining heat to complete the desorption of water in the adsorption material with low-temperature desorption performance; after the hot blowing is completed, the high-temperature regeneration gas is stopped, and then the cold blowing gas is introduced to cool the adsorption layer. The cold blowing gas flows through each adsorption layer in the same flow direction as the hot blowing. Both the hot blowing desorption gas and the cold blowing gas are discharged through the adsorption inlet pipe (1).

7. The method of use according to claim 6, characterized in that: During the desorption stage, the inlet temperature of the high-temperature regeneration gas is 180-220℃. After flowing through the inner adsorption layer (10), the temperature drops to 140-160℃. After flowing through the middle adsorption layer (9), the temperature drops to 100-120℃. After flowing through the outer adsorption layer (8), the temperature drops to below 80℃.

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