Heat exchange type temperature swing adsorption column and adsorption method

Abstract

The present application relates to a kind of heat exchange type temperature swing adsorption tower, including lower port, lower head, tower body, upper head and upper port, the tower body is cylindrical shell, tower body is sequentially communicated upper port, upper head, lower head and lower port from top to bottom, the vertical space in the tower body is adsorption zone, and arc heat exchange tube bundle is arranged in adsorption zone, the arc heat exchange tube bundle is by the longitudinal and transverse heat exchange tube bundle network that multiple groups " straight pipe " of " arch " shape arrangement is constituted, the arc heat exchange tube bundle is connected to heat exchange manifold inlet in the upper portion of tower body, and is connected to heat exchange manifold outlet in the lower portion of tower body, the opening direction of horizontal section of the arc heat exchange tube bundle is provided with manhole on the tower body, the present application has the beneficial effect that the disturbance of arc heat exchange tube bundle, make raw material gas and desorption gas distribution more uniform, adsorbent absorption and desorption regeneration effect is better, it is convenient to adsorbent packing, adsorption tower service life increases, operating cost is reduced.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of raw gas impurity swing adsorption, and particularly relates to a heat exchange type swing adsorption tower and an adsorption method. BACKGROUND

[0002] Temperature swing adsorption (TSA) is an adsorption separation technology, which realizes the separation and purification of target components based on the change of adsorption capacity of adsorbents to target components at different temperatures. The temperature swing adsorption technology has the advantages of flexible operation, low energy consumption, good separation effect, etc., and has been widely used in many fields.

[0003] In the process of raw gas temperature swing adsorption, but during desorption and regeneration, a large amount of desorption gas needs to be heated by using a heat source first, and then the bed is heated by using the heated desorption gas, and finally the desorption gas is cooled. This indirect heating method of the bed by using the desorption gas will result in low heat efficiency and high energy consumption, low utilization rate of temperature swing adsorption, high energy consumption, and difficulty in filling adsorption filler.

[0004] A Chinese invention patent with the publication number CN116328485A discloses a hydrogen temperature swing adsorption impurity removal device and hydrogen temperature swing adsorption impurity removal process. The device improves the heat exchange and mass transfer efficiency through the structures of annular tube bundle and multiple heat exchange tubes. However, the space inside the tower is complex, which not only has low space utilization rate, but also increases the difficulty of packing the adsorbent. The heat exchange tube with a cage structure makes it difficult to uniformly fill the adsorption filler inside. Moreover, the entire adsorption impurity removal device is a one-time closed structure, and the adsorption filler cannot be supplemented during the adsorption process. As the adsorption process consumes the adsorption filler, it cannot be supplemented, and eventually needs to be re-made. The device has low utilization rate and high operation cost, which is not conducive to popularization. SUMMARY

[0005] In order to overcome the shortcomings of the prior art, the present application provides a heat exchange type swing adsorption tower and an adsorption method. The longitudinal and transverse heat exchange network in the tower is mainly composed of multiple groups of “straight pipes” arranged in the shape of a “bow”. The heat expansion and contraction compensation ability of the naturally formed “bow” shaped heat exchange tube bundle reduces thermal stress. The “bow” shaped heat exchange tube bundle lengthens the heat exchange path, and the residence time of the heat exchange medium in the adsorption zone is longer, which increases the desorption and regeneration capacity. The platform area formed at the horizontal opening of the “bow” shape facilitates the packing of the adsorption filler. The adsorption filler can be supplemented at any time during the adsorption process. The gaps between the tube bundles can also be used for the passage of raw gas and desorption gas, and the disturbance formed can make the flow field distribution in the tower more uniform.

[0006] In order to achieve the above purpose, the present application adopts the following technical scheme:

[0007] A heat exchange type temperature swing adsorption tower, comprising a lower port, a lower head, a tower body, an upper head and an upper port, the tower body is a cylindrical barrel, the tower body is sequentially communicated with the upper port, the upper head, the lower head and the lower port from top to bottom, the vertical space in the tower body is an adsorption zone, an arc-shaped heat exchange tube bundle is arranged in the adsorption zone, the arc-shaped heat exchange tube bundle is composed of a longitudinal and transverse heat exchange tube bundle network formed by a plurality of groups of "straight tubes" arranged in an "arch" shape, the arc-shaped heat exchange tube bundle is connected to a heat exchange main pipe inlet at the upper part of the tower body and connected to a heat exchange main pipe outlet at the lower part of the tower body, and a manhole is arranged on the tower body in the opening direction of the horizontal section of the arc-shaped heat exchange tube bundle.

[0008] Further, the heat exchange type temperature swing adsorption tower further comprises an upper distributor, an inter-tube gas distribution disc and a lower distributor, the upper distributor is arranged in the internal connection between the upper head and the lower end of the tower body, the lower distributor is arranged in the internal connection between the lower head and the lower end of the tower body, and the inter-tube gas distribution disc is arranged in the middle of the internal of the tower body.

[0009] Further, the heat exchange main pipe inlet and the heat exchange main pipe outlet extend out of the tower body.

[0010] Further, an outlet filter is arranged in the upper port.

[0011] Further, the upper distributor adopts a flat plate shape and adopts a porcelain ball or mechanical compression structure.

[0012] Further, the lower distributor adopts a flat plate shape when the diameter of the adsorption tower is less than or equal to 2 m.

[0013] Further, the lower distributor adopts a frustum shape when the diameter of the adsorption tower is greater than 2 m, and gas holes are arranged on the top and side surface of the frustum.

[0014] Further, the adsorption method of the heat exchange type temperature swing adsorption tower is as follows:

[0015] S1, filling: the adsorption filler is pushed into the internal of the tower body through the lower manhole, the adsorption filler is compacted through the lowermost manhole, and then the adsorption filler is pushed into the tower body through the manholes on both sides of the tower body from bottom to top, since the manhole is directly opposite the horizontal opening of the arc-shaped heat exchange tube bundle, the filler compaction equipment can be inserted into the internal of the tower body, and the internal of the tower body is filled with compacted adsorption filler;

[0016] S2, impurity removal; raw material gas enters the adsorption tower from the lower port, sequentially passes through the lower distributor, adsorption zone, inter-tube gas distribution disc, upper distributor, outlet filter and upper port from bottom to top, while the raw material gas is adsorbed by the adsorption filler in the adsorption zone to remove impurities, the raw material gas is evenly distributed by the lower distributor, inter-tube gas distribution disc and lower distributor, the rising flow rate of the raw material gas is slowed down, and trace amounts of tar, benzene, naphthalene, hydrogen sulfide, ammonia, hydrogen cyanide and part of organic sulfur in the raw material gas are removed by adsorption and then filtered and purified by the outlet filter to complete the adsorption and purification of the raw material gas;

[0017] S3, pressure relief; when the adsorption capacity of the adsorbent approaches adsorption saturation, the upper port is closed, and the lower port is opened at the same time, so that the adsorption tower is reversely depressurized to reduce the tower pressure to normal pressure;

[0018] S4, desorption regeneration; when the adsorption tower is reduced to normal pressure, the upper port is opened to make the desorption gas flow in, and the desorption gas sequentially passes through the upper distributor, adsorption zone, inter-tube gas distribution disc, lower distributor and lower port from top to bottom; at the same time, the heat exchange main pipe inlet is opened, and the heating medium is introduced, so that the adsorbent and the desorption gas are heated by the heating medium, the heating medium is discharged from the heat exchange main pipe outlet after being cooled, and the impurity gas desorbed from the adsorbent is discharged from the lower port together with the desorption gas;

[0019] S5, cooling; after the desorption regeneration is completed, the cooling medium is introduced from the heat exchange main pipe inlet, so that the cooling medium flows through the arc-shaped heat exchange tube bundle, the cooling medium is discharged from the heat exchange main pipe outlet after being heated, and the purge gas still blows the residual gas in the adsorption zone from top to bottom and is discharged from the lower port;

[0020] S6, material supplementing; the manhole outside the uppermost tower body is opened, whether the adsorption filler in the uppermost adsorption zone fills the entire adsorption zone is observed, and if there is an adsorption filler cavity, the adsorption filler is filled into the tower body by using the filler equipment;

[0021] S7, final filling; the heat exchange main pipe inlet and outlet and the lower port are closed, the desorption gas of the upper port is used to charge the tower, until the adsorbent in the adsorption zone reaches the adsorption pressure, the upper port is closed, and thus one temperature swing adsorption cycle is completed.

[0022] Compared with the prior art, the beneficial effects of the present application are:

[0023] 1. The arc-shaped heat exchange tube bundle is arranged in the adsorption tower, indirect heating and cooling of the temperature swing adsorption process are realized, the use amount of regeneration desorption gas is reduced while ensuring the recycling of the heating and cooling medium; the disturbance of the arc-shaped heat exchange tube bundle makes the distribution of the raw material gas and the desorption gas more uniform, and the adsorbent absorption and desorption regeneration effect is better.

[0024] 2. The heat exchange tube itself has the compensation ability of thermal expansion and contraction, reduces the thermal stress, and the horizontal opening position of the "arch" shape forms a platform area, which facilitates the adsorbent filling, the adsorbent filling can be supplemented at any time, the service life of the adsorption tower is increased, and the operation cost is reduced.

[0025] 3. The "arch" shape straight tube bundle is convenient to manufacture and process, low in cost, easy to maintain, and small in flow resistance, and thus is particularly suitable for the adsorption process of coke oven gas and other corrosive gases.

[0026] 4. The upper distributor, the inter-tube gas distribution disc and the lower distributor are arranged in the tower body, so that the raw material gas and the desorption gas are uniformly distributed after being uniformly dispersed and the running speed of the raw material gas and the desorption gas in the adsorption area of the tower body is reduced, the adsorption time and the desorption regeneration time are prolonged, the raw material gas adsorption is more thorough, the desorption regeneration is more sufficient, and the utilization rate of the adsorption filler is higher. BRIEF DESCRIPTION OF DRAWINGS

[0027] Figure 1 is a heat exchange type adsorption tower structure diagram according to the present application.

[0028] Figure 2 is a left view of the heat exchange type adsorption tower according to the present application.

[0029] Figure 3 is a top view of the heat exchange type adsorption tower according to the present application.

[0030] Figure 4 is a sectional view of the heat exchange type adsorption tower according to the present application.

[0031] Figure 5 is a conical frustum-shaped lower distributor adsorption tower structure diagram according to the present application.

[0032] Figure 6 is an axial side view of the heat exchange type adsorption tower according to the present application.

[0033] Figure 7 is a gas flow field distribution diagram of the heat exchange type adsorption tower according to the present application.

[0034] Figure 8 is a line diagram of the gas flow field of the heat exchange type adsorption tower according to the present application.

[0035] In the figure: 1. lower port, 2. lower head, 3. lower distributor, 4. tower body, 5. arch-shaped heat exchange tube bundle, 6. adsorption area, 7. upper distributor, 8. outlet filter, 9. upper head, 10. upper port, 20. inter-tube gas distribution disc, 21. heat exchange main pipe inlet, 22. heat exchange main pipe outlet, 31. manhole DETAILED DESCRIPTION

[0036] The specific embodiments of the present invention will be further described below with reference to the accompanying drawings:

[0037] like Figures 1-8 As shown, the working principle of a heat exchange type variable temperature adsorption tower is as follows: Raw material gas enters through the lower port 1 of the adsorption tower. Tar, benzene, naphthalene, hydrogen sulfide, ammonia, hydrogen cyanide, and some organic sulfur in the raw material gas are adsorbed and removed by the adsorption packing material in the adsorption zone. The purified raw material gas is output from the upper port 10. When the adsorption packing material reaches its adsorption limit, desorption gas enters through the upper port 10. The heat exchange medium is introduced through the arc-shaped heat exchange tube bundle 5 to heat the desorption gas and the adsorption packing material, causing the adsorption packing material to desorb and regenerate. Impurity gases are discharged from the lower port 1 along with the desorption gas. The manhole 31 is located at the horizontal opening of the arc-shaped heat exchange tube bundle 5, facilitating adsorption agent loading and allowing for timely replenishment of the adsorption packing material. This increases the service life of the adsorption tower and reduces operating costs.

[0038] like Figures 1-8 As shown, a heat exchange type variable temperature adsorption tower includes a lower port 1, a lower end cap 2, a tower body 4, an upper end cap 9, and an upper port 10. The tower body 4 is a cylindrical shell, and the upper port 10, upper end cap 9, lower end cap 2, and lower port 1 are connected sequentially from top to bottom. The upper end cap 9 and lower end cap 1 adopt an arc transition connection structure. The vertical space inside the tower body 4 is an adsorption zone 6. An arc-shaped heat exchange tube bundle 5 is arranged in the adsorption zone 6. The heating and cooling media in the arc-shaped heat exchange tube bundle 5 can heat and cool the adsorbent. While ensuring the recycling of the heating and cooling media, the heating efficiency is improved and the amount of regeneration desorption gas used is reduced. Due to the disturbance effect of the bow-shaped heat exchange tube bundle 5 inside the adsorption tower, the distribution of raw gas and desorbed gas is more uniform, and the adsorbent absorption and desorption effects are better. The bow-shaped heat exchange tube bundle 5 is composed of a longitudinal and transverse heat exchange tube network consisting of multiple sets of straight tubes arranged in a "bow" shape. The bow-shaped heat exchange tube bundle 5 converges at the upper part of the tower body 4 and connects to the heat exchange main pipe inlet 21, and converges at the lower part of the tower body 4 and connects to the heat exchange main pipe outlet 22. After the heat exchange main pipe inlet 21 extends into the tower through the shell below the upper end cap 9, it branches into several horizontal and perpendicular branches to the heat exchange main pipe inlet 21. The horizontal tube bundles extend horizontally to a distance of 1.5DN from the inner wall of the tower body 4, then bend 90 degrees vertically downwards. The drooping height is calculated according to H = a·B (a-1~2; B-length of the horizontal section of the bow-shaped heat exchange tube bundle 5; H-length of the vertical section of the bow-shaped heat exchange tube bundle 5). That is, the drooping height of the bow-shaped heat exchange tube bundle 5 is 1 to 2 times the horizontal extension distance. When the bow-shaped heat exchange tube bundle 5 reaches the drooping height, it bends 90 degrees in the opposite direction and becomes a horizontal tube bundle section again. The above steps are repeated until it is connected to the heat exchange main outlet 22 above the lower head 2.

[0039] To avoid thermal stress caused by pipe expansion and contraction due to temperature changes during start-up and shutdown, the bow-shaped heat exchanger tube bundle 5 is pre-drawn during installation to ensure that the sway amplitude under maximum tensile stress and compressive stress is equal.

[0040] ΔL / 2 = ΔL1 + ΔL2

[0041] ΔL1 = ΔL2

[0042] In the formula: ΔL - compensation length of the arc heat exchange tube, mm

[0043] ΔL1 - swing of each vertical arm of the arc heat exchange tube under the action of maximum tensile stress, mm

[0044] ΔL2 - swing of each vertical arm of the arc heat exchange tube under the action of maximum compressive stress, mm

[0045] The manholes 31 are arranged on the tower body 4 in the horizontal section opening direction of the arc heat exchange tube bundle 5, which are used for entering and exiting the tower body 4 and loading the adsorption filler at the corresponding position, and the vertical space formed in the tower body between the lower head 2 and the upper head 9 is the main adsorption zone 6 for the adsorption and impurity removal of the raw gas and the temperature rising desorption, and the adsorption filler filled here bears the main adsorption and separation function, and the adsorption zone 6 is filled with the adsorption filler, which includes but is not limited to activated carbon, silica gel, molecular sieve and the like according to the gas purification requirement.

[0046] Further, the heat exchange type temperature swing adsorption tower further comprises an upper distributor 7, an inter-tube gas distribution disc 20 and a lower distributor 3, the upper distributor 7 is arranged in the internal connection between the upper head 9 and the lower end of the tower body 10, the lower distributor 3 is arranged in the internal connection between the lower head 2 and the lower end of the tower body 4, and the inter-tube gas distribution disc 20 is arranged in the middle of the tower body 4.

[0047] Further, the heat exchange main pipe inlet 21 and the heat exchange main pipe outlet 22 extend out of the tower body 4.

[0048] Further, the outlet filter 8 is arranged in the upper end port 10.

[0049] Further, the upper distributor 7 corresponds to the upper end port 10 of the adsorption tower, adopts a flat plate shape, the flat plate distributor is a layer to a plurality of hole plates, and the hole plate adopts a porcelain ball or mechanical compression structure to prevent the fluidization of the adsorption bed.

[0050] Further, the lower distributor 3 adopts a flat plate shape when the diameter of the adsorption tower is less than or equal to 2 m.

[0051] Further, the adsorption method of the heat exchange type temperature swing adsorption tower is as follows:

[0052] S1, filling: the adsorption filler is pushed into the tower body 4 through the lower manhole 31, and the adsorption filler is compacted through the lowermost manhole 31, and then the adsorption filler is pushed into the tower body 4 through the manholes 31 from bottom to top in turn. Since the manhole 31 is opposite to the horizontal opening of the arc-shaped heat exchange tube bundle 5, the filler compaction device can be inserted into the tower body 4 to fill the tower body 4 with compacted adsorption filler;

[0053] S2, impurity removal: the raw gas enters the adsorption tower from the lower port 1, sequentially passes through the lower distributor 3, the adsorption zone 6, the inter-tube gas distribution disc 20, the upper distributor 7, the outlet filter 8 and the upper port 10 from bottom to top, and the raw gas is evenly distributed through the lower distributor 3, the inter-tube gas distribution disc 20 and the upper distributor 7 while the impurities in the raw gas are adsorbed by the adsorption filler in the adsorption zone 6, so as to slow down the rising flow rate of the raw gas. After the trace amounts of tar, benzene, naphthalene, hydrogen sulfide, ammonia, hydrogen cyanide and part of organic sulfur in the raw gas are removed by adsorption, the raw gas is filtered and purified through the outlet filter 8 to complete the adsorption and purification of the raw gas;

[0054] S3, pressure relief: when the adsorption capacity of the adsorbent approaches adsorption saturation, the upper port 10 is closed, and the lower port 1 is opened at the same time to perform reverse pressure relief on the adsorption tower, so that the tower pressure is reduced to normal pressure;

[0055] S4, desorption and regeneration: when the adsorption tower is reduced to normal pressure, the upper port 10 is opened to make the desorption gas flow in, and the desorption gas sequentially passes through the upper distributor 7, the adsorption zone 6, the inter-tube gas distribution disc 20, the lower distributor 3 and the lower port 1 from top to bottom. At the same time, the heat exchange main pipe inlet 21 is opened to introduce the heating medium, and the adsorbent and the desorption gas are heated by the heating medium. After the heating medium is cooled, it is discharged from the heat exchange main pipe outlet 22, and the impurity gas desorbed from the adsorbent is discharged from the lower port together with the desorption gas;

[0056] S5, cooling: after the desorption and regeneration are completed, the cooling medium is introduced from the heat exchange main pipe inlet 21 to flow through the arc-shaped heat exchange tube bundle, and the cooling medium is discharged from the heat exchange main pipe outlet 22 after being heated. The purge gas still blows the residual gas in the adsorption zone 6 from top to bottom and is discharged from the lower port 1;

[0057] S6, feeding: the uppermost manhole 21 outside the tower body 4 is opened to observe whether the adsorption filler in the uppermost adsorption zone fills the entire adsorption zone 6. If there is a hollow space in the adsorption filler, the filler device is used to fill the adsorption filler into the tower body;

[0058] S7, final filling: the heat exchange main pipe inlet and outlet and the lower port 1 are closed, and the desorption gas of the upper port 10 is used to charge the tower until the adsorbent in the adsorption zone 6 reaches the adsorption pressure. The upper port 1 is closed, and thus a temperature swing adsorption cycle is completed.

[0059] The above description is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any equivalent substitutions or modifications made by those skilled in the art within the scope of the technology disclosed in the present invention, based on the technical solution and concept of the present invention, should be covered within the scope of protection of the present invention.

[0060] The following embodiments are implemented based on the technical solution of the present invention, providing detailed implementation methods and specific operation processes. However, the scope of protection of the present invention is not limited to the following embodiments. Unless otherwise specified, the methods used in the following embodiments are conventional methods.

[0061]

Example

[0062] like Figures 5-6 As shown, the actual volumetric flow rate of coke oven gas is 12716 m³ / s. 3 The calculated tower diameter is 3.6m. Since the tower diameter is greater than 2m, a frustum-shaped distributor is selected for the lower distributor 3. This type of distributor has the advantages of small void volume, strong support capacity, and a large amount of adsorbent in the head. Gas holes are opened on the top and sides of the frustum. Based on the above calculation of coke oven gas impurity content and adsorption time of 6 hours, the total impurity adsorption capacity is 8.5t. If the adsorption capacity is 40% and the surplus coefficient is taken as 1.25, the total adsorbent loading is calculated to be 27t. If the bulk density is 520kg / m³, the total adsorbent loading is 27t. 3 When considering this, the required packing volume is 52m³. 3 The filling height was calculated to be 5m based on the tower diameter, thus determining the distance between the heat exchanger inlet 21 and the heat exchanger outlet 22 to be 5m.

[0063] Calculated using H = a·B, the horizontal section length of the arc-shaped heat exchange tube bundle 5 is 1m, the vertical section length is 1m, there are four horizontal openings, and four manholes 31 are located on both sides of the tower body.

[0064] Starting from the bottom manhole 31, adsorption packing is filled into the adsorption zone 6 inside the tower body 4. After compaction at the manhole 31, the adsorption packing continues to be filled upward through the manhole 31 until the entire adsorption zone 6 is filled with adsorption packing.

[0065] The raw gas enters through the lower port 1 of the adsorption tower. After the raw gas passes through the upper distributor 7, the inter-pipe gas distribution disk 20 and the lower distributor 3 to equalize the pressure and slow down the upward speed, it slowly passes through the adsorption zone 6. The adsorption packing in the adsorption zone 6 adsorbs and removes tar, benzene, naphthalene, as well as hydrogen sulfide, ammonia, hydrogen cyanide and some organic sulfur from the raw gas. The purified raw gas is then output from the upper port 10.

[0066] When the adsorption filler reaches the adsorption limit, desorption gas enters from the upper port 10, passes through the arc-shaped heat exchange pipe bundle 5, and enters the heat exchange medium to heat the desorption gas and the adsorption filler, so that the adsorption filler is desorbed and regenerated, and the impurity gas is discharged from the lower port 1 together with the desorption gas. The manhole is arranged at the horizontal opening position of the arc-shaped heat exchange pipe bundle 5, which facilitates the filling of the adsorbent, the service life of the adsorption tower is increased, and the operation cost is reduced.

Claims

1. A heat exchange type variable temperature adsorption tower, comprising a lower port, a lower end cap, a tower body, an upper end cap, and an upper port, wherein the tower body is a cylindrical shell, and the upper port, upper end cap, lower end cap, and lower port are sequentially connected from top to bottom within the tower body, characterized in that, The vertical space inside the tower is the adsorption zone, and an arc-shaped heat exchange tube bundle is installed in the adsorption zone. The arc-shaped heat exchange tube bundle is composed of a longitudinal and transverse heat exchange tube bundle network consisting of multiple sets of straight tubes arranged in an "arch" shape. The arc-shaped heat exchange tube bundles converge at the upper part of the tower and connect to the inlet of the heat exchange main pipe, and converge at the lower part of the tower and connect to the outlet of the heat exchange main pipe. A manhole is provided on the tower body in the horizontal opening direction of the arc-shaped heat exchange tube bundle. The heat exchange type variable temperature adsorption tower further includes an upper distributor, an inter-tube gas distributor, and a lower distributor. The upper distributor is located inside the connection between the upper end cap and the upper end of the tower body, and the lower distributor is located inside the connection between the lower end cap and the lower end of the tower body. The inter-tube gas distributor is located in the middle of the tower body. The upper distributor is flat and uses a ceramic ball or mechanically compressed structure. The lower distributor is flat when the adsorption tower diameter is ≤2m; the lower distributor is frustoconical when the adsorption tower diameter is >2m, with gas holes on the top and sides of the frustocone. The horizontal tube bundle section of the arc-shaped heat exchanger tube bundle extends horizontally to 1.5DN from the inner wall of the tower body, then bends 90 degrees vertically downwards. The downward height is calculated according to H=a·B, where a: 1~2; B: length of the horizontal section of the arc-shaped heat exchanger tube bundle; H: length of the vertical section of the arc-shaped heat exchanger tube bundle. When installing the bow-shaped heat exchanger tube bundle, it is pre-drawn to ensure that the sway amplitude under maximum tensile stress and compressive stress is equal. Where: ΔL—compensation length of the arc-shaped heat exchange tube, mm; ΔL1—The sway amplitude of each vertical arm of the arc-shaped heat exchanger tube under maximum tensile stress, in mm; ΔL2—the swing amplitude of each vertical arm of the bow-shaped tube under maximum compressive stress, in mm.

2. The heat exchange type variable temperature adsorption tower according to claim 1, characterized in that, The heat exchanger inlet and outlet extend outside the tower body.

3. The heat exchange type variable temperature adsorption tower according to claim 1, characterized in that, An outlet filter is installed inside the upper port.

4. An adsorption method for a heat exchange type variable temperature adsorption tower as described in claim 1, characterized in that, The adsorption method of the heat exchange type variable temperature adsorption tower is as follows: S1. Packing: The adsorption packing is pushed into the tower body through the lower manhole, and the adsorption packing is compacted through the bottommost manhole. Then, the adsorption packing is pushed in through the manholes on both sides of the tower body from bottom to top. Since the manhole is directly opposite the horizontal opening of the arc-shaped heat exchange tube bundle, the packing compaction equipment can be extended into the tower body to fill and compact the adsorption packing inside the tower body. S2. Impurity Removal: The raw gas enters the adsorption tower from the lower port and passes sequentially from bottom to top through the lower distributor, adsorption zone, inter-pipe gas distributor, upper distributor, outlet filter, and upper port. While the raw gas passes through the adsorption packing in the adsorption zone to adsorb impurities, it passes through the lower distributor, inter-pipe gas distributor, and lower distributor to equalize the pressure of the raw gas and slow down the rising outflow velocity of the raw gas. Trace amounts of tar, benzene, naphthalene, as well as hydrogen sulfide, ammonia, hydrogen cyanide, and some organic sulfur in the raw gas are adsorbed and removed. After being smoothly filtered and purified by the outlet filter, the adsorption and purification of the raw gas is completed. S3, Pressure Relief: When the adsorption capacity of the adsorbent is close to adsorption saturation, close the upper port and open the lower port at the same time to reverse the pressure of the adsorption tower and reduce the tower pressure to atmospheric pressure. S4. Desorption and Regeneration: After the adsorption tower is reduced to atmospheric pressure, the upper port is opened to allow the desorbed gas to flow in. The desorbed gas passes through the upper distributor, adsorption zone, inter-tube gas distributor, lower distributor, and lower port in sequence from top to bottom. At the same time, the inlet of the heat exchange manifold is opened and the heating medium is introduced to heat the adsorbent and desorbed gas. After the heating medium cools down, it is discharged from the outlet of the heat exchange manifold. The impurity gas desorbed by the adsorbent and the desorbed gas are discharged together from the lower port. S5. Cooling: After desorption and regeneration are completed, cooling medium is introduced from the inlet of the heat exchange manifold, so that the cooling medium flows through the bow-shaped heat exchange tube bundle. After the cooling medium is heated, it is discharged from the outlet of the heat exchange manifold. The purging gas continues to purge the residual gas in the adsorption zone from top to bottom and is discharged from the bottom port. S6. Feeding: Open the manhole on the outside of the top tower body and observe whether the adsorption packing in the top adsorption zone fills the entire adsorption zone. If voids are found in the adsorption packing, use the packing equipment to fill the tower body with adsorption packing. S7. Final charge: Close the inlet and outlet of the heat exchange main and the lower port, and use the desorption gas from the upper port to pressurize the tower until the adsorbent in the adsorption zone reaches the adsorption pressure. Then close the upper port to complete one temperature-switching adsorption cycle.

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