Heat exchange type temperature swing adsorption tower

Abstract

The utility model relates to a heat exchange type temperature swing adsorption tower which comprises a lower port, a lower seal head, a tower body, an upper seal head and an upper port, the tower body is a cylindrical barrel, the tower body is sequentially communicated with the upper port, the upper seal head, the lower seal head and the lower port from top to bottom, a vertical space in the tower body is an adsorption area, an arch-shaped heat exchange tube bundle is arranged in the adsorption area, and the arch-shaped heat exchange tube bundle is arranged in the adsorption area. The arch-shaped heat exchange tube bundles are composed of a plurality of groups of vertical and horizontal heat exchange tube bundle networks formed by straight tubes arranged in an arch shape, the arch-shaped heat exchange tube bundles are gathered at the upper part of the tower body and are connected to an inlet of the heat exchange main tube, and the arch-shaped heat exchange tube bundles are gathered at the lower part of the tower body and are connected to an outlet of the heat exchange main tube, and manholes are formed in the tower body in the opening direction of the horizontal sections of the arch-shaped heat exchange tube bundles. The adsorption tower has the beneficial effects that raw material gas and desorbed gas are distributed more uniformly under the disturbance action of the arched heat exchange tube bundle, the absorption and desorption regeneration effects of an adsorbent are better, the adsorbent is convenient to fill, the service life of the adsorption tower is prolonged, and the operation cost is reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of raw gas impurity temperature swing adsorption, in particular to a heat exchange type temperature swing adsorption tower. Background Technique

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

[0003] During the process of raw gas temperature swing adsorption, however, during desorption and regeneration, it is necessary to first use a heat source to heat a large amount of desorbed gas, then use the hot desorbed gas to heat the bed layer, and finally cool the desorbed gas. This way of indirectly heating the bed layer by using desorbed gas will lead to low thermal efficiency, high energy consumption, low utilization rate of temperature swing adsorption, high energy consumption, and difficulty in filling adsorption packing.

[0004] The Chinese invention patent with the application publication number of CN116328485A discloses "a hydrogen temperature swing adsorption impurity removal device and a hydrogen temperature swing adsorption impurity removal process". Through structures such as annular "tube bundles" and multiple heat exchange tubes, the heat exchange and mass transfer efficiency are improved. The space inside the tower is complicated, not only the space utilization rate is low, but also the loading difficulty of the adsorbent is increased. The heat exchange tubes with a cage structure make it difficult to evenly fill the adsorption packing inside. Moreover, the entire adsorption impurity removal device is a one-time closed structure, and the packing cannot be supplemented during the adsorption process. As the adsorption process progresses, the consumed adsorption packing cannot be supplemented, and finally it needs to be remade. The device utilization rate is low, the operation cost is high, and it is not conducive to popularization. Summary of the Invention

[0005] In order to overcome the deficiencies of the prior art, the utility model provides a heat exchange type temperature swing adsorption tower. The vertical and horizontal heat exchange network in the tower is mainly composed of multiple groups of "straight tubes" arranged in a "bow" shape. The natural thermal expansion and contraction compensation ability formed by the "bow" shaped heat exchange tube bundles reduces thermal stress. The "bow" shaped heat exchange tube bundles lengthen the heat exchange path, increase the residence time of the heat exchange medium in the adsorption area, and increase the desorption and regeneration ability. The platform area formed at the horizontal opening of the "bow" shape is convenient for filling the adsorption packing, and the packing can be supplemented at any time during the adsorption process. The gaps between the tube bundles can also allow the raw gas and desorbed gas to pass through, and the formed disturbance can make the flow field distribution inside the tower more uniform.

[0006] In order to achieve the above purpose, the utility model adopts the following technical solutions:

[0007] A heat exchange type temperature-swing adsorption tower comprises a lower port, a lower head, a tower body, an upper head and an upper port. The tower body is a cylindrical barrel, and the tower body is connected to the upper port, the upper head, the lower head and the lower port in sequence from top to bottom. The vertical space in the tower body is an adsorption zone, and an arched heat exchange tube bundle is arranged in the adsorption zone. The arched heat exchange tube bundle is composed of a longitudinal and transverse heat exchange tube bundle network composed of multiple groups of "straight tubes" arranged in a "bow" shape. The arched heat exchange tube bundle is connected to the inlet of the heat exchange main pipe at the upper part of the tower body and to the outlet of the heat exchange main pipe at the lower part of the tower body. A manhole is arranged on the tower body in the opening direction of the horizontal section of the arched heat exchange tube bundle.

[0008] Furthermore, the heat exchange type temperature swing adsorption tower also includes an upper distributor, an inter-tube gas distributor and a lower distributor. The upper distributor is arranged inside the connection between the upper head and the upper end of the tower body, the lower distributor is arranged inside the connection between the lower head and the lower end of the tower body, and the inter-tube gas distributor is arranged in the middle of the tower body.

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

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

[0011] Furthermore, the upper distributor is in the shape of a flat plate and adopts a porcelain ball or mechanically compressed structure.

[0012] Furthermore, the lower distributor is in a flat plate shape when the adsorption tower diameter is ≤2m.

[0013] Furthermore, when the diameter of the adsorption tower is greater than 2 m, the lower distributor is in the shape of a frustum, with gas holes opened on the top and sides of the frustum.

[0014] Compared with the prior art, the beneficial effects of the utility model are:

[0015] 1. The present invention arranges an arcuate heat exchange tube bundle in the adsorption tower to realize indirect heating and cooling in the temperature swing adsorption process, while ensuring the recycling of heating and cooling media, reducing the amount of regeneration desorption gas; the disturbance effect of the arcuate heat exchange tube bundle makes the distribution of raw gas and desorption gas more uniform, and the adsorbent absorption and desorption regeneration effect is better.

[0016] 2. The "bow"-shaped heat exchange tube itself has the ability to compensate for thermal expansion and contraction, reducing the generation of thermal stress. The horizontal opening position of the "bow" shape can also form a platform area, which is convenient for adsorbent loading and the adsorption filler can be replenished at any time. The service life of the adsorption tower is increased and the operating cost is reduced.

[0017] 3. The "bow"-shaped straight tube bundle is easy to manufacture and process, has low cost, is easy to maintain, and has low flow resistance. Therefore, it is particularly suitable for the adsorption process of corrosive gases such as coke oven gas.

[0018] 4. The upper distributor, the inter-tube gas distributor and the lower distributor are arranged inside the tower body to equalize and disperse the raw material gas and the desorbed gas in the tower body, evenly distribute them, reduce the running speed of the raw material gas and the desorbed gas in the adsorption zone of the tower body, extend the adsorption time and the desorption and regeneration time, so that the raw material gas is adsorbed more thoroughly, the desorption and regeneration is more sufficient, and the utilization rate of the adsorption packing is higher. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] Figure 1 It is a schematic structural diagram of a heat exchange type variable temperature adsorption tower according to the present utility model.

[0020] Figure 2 It is a left view of the heat exchange type variable temperature adsorption tower according to the present utility model.

[0021] Figure 3 It is a top view of the heat exchange type variable temperature adsorption tower according to the present utility model.

[0022] Figure 4 It is a sectional view of the heat exchange type variable temperature adsorption tower according to the present utility model.

[0023] Figure 5 It is a schematic structural diagram of a variable temperature adsorption tower with a frustum-shaped lower distributor according to the present utility model.

[0024] Figure 6 It is an axonometric view of the heat exchange type variable temperature adsorption tower according to the present utility model.

[0025] Figure 7 It is a gas flow field distribution diagram of the heat exchange type variable temperature adsorption tower according to the present utility model.

[0026] Figure 8 It is a line graph of the gas flow field of the heat exchange type variable temperature adsorption tower according to the present utility model.

[0027] In the figure: 1. lower port, 2. lower head, 3. lower distributor, 4. tower body, 5. bow-shaped heat exchange tube bundle, 6. adsorption zone, 7. upper distributor, 8. outlet filter, 9. upper head, 10. upper port, 20. inter-tube gas distributor, 21. inlet of heat exchange main pipe, 22. outlet of heat exchange main pipe, 31. manhole DETAILED DESCRIPTION OF THE EMBODIMENTS

[0028] The following further describes the specific embodiments of the present utility model with reference to the drawings:

[0029] As Figures 1-8As shown in the figure, the working principle of a heat exchange type variable temperature adsorption tower is as follows: The raw 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 gas are adsorbed and removed by the adsorption packing in the adsorption zone. The purified raw gas is output from the upper port 10. When the adsorption packing reaches the adsorption limit, the desorbing gas enters through the upper port 10. The heat exchange medium is passed through the bow-shaped heat exchange tube bundle 5 to heat the desorbing gas and the adsorption packing, so that the adsorption packing is desorbed and regenerated. The impurity gas and the desorbing gas are discharged together from the lower port 1. The manhole 31 is arranged at the horizontal opening position of the bow-shaped heat exchange tube bundle 5, which is convenient for filling the adsorbent, can supplement the adsorption packing at any time, increases the service life of the adsorption tower, and reduces the operating cost.

[0030] As Figures 1-8 shown, a heat exchange type variable temperature adsorption tower includes a lower port 1, a lower head 2, a tower body 4, an upper head 9, and an upper port 10. The tower body 4 is a cylindrical barrel. The tower body 4 is connected in series with the upper port 10, the upper head 9, the lower head 2, and the lower port 1 from top to bottom. The upper head 9 and the lower head 1 adopt an arc transition connection structure. The vertical space inside the tower body 4 is the adsorption zone 6. The bow-shaped heat exchange tube bundle 5 is arranged in the adsorption zone 6. The heating and cooling media in the bow-shaped heat exchange tube bundle 5 can heat and cool the adsorbent, while ensuring the recycling of the heating and cooling media, improving the heating efficiency and reducing the amount of desorbing gas for regeneration. Due to the disturbance of the bow-shaped heat exchange tube bundle 5 in the adsorption tower, the distribution of the raw gas and the desorbing gas is more uniform, and the absorption and desorption effects of the adsorbent are better. The bow-shaped heat exchange tube bundle 5 is composed of a vertical and horizontal heat exchange tube network formed by multiple groups of "straight tubes" arranged in a "bow" shape. The bow-shaped heat exchange tube bundle 5 is connected to the inlet of the heat exchange main pipe 21 at the upper part of the tower body 4 and to the outlet of the heat exchange main pipe 22 at the lower part of the tower body 4. After the inlet of the heat exchange main pipe 21 penetrates the shell and extends into the tower below the upper head 9, it branches into several horizontal tube segments perpendicular to the inlet of the heat exchange main pipe 21. These horizontal tube segments extend horizontally to a distance of 1.5DN from the inner wall of the tower body 4 and then bend 90 degrees vertically downward. The hanging height is calculated according to H = a·B (a - 1 to 2; B - the horizontal length of the bow-shaped heat exchange tube bundle 5; H - the vertical length of the bow-shaped heat exchange tube bundle 5), that is, the hanging 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 hanging height, it bends 90 degrees in the opposite direction and becomes a horizontal tube segment again, repeating the above steps until it is connected to the outlet of the heat exchange main pipe 22 above the lower head 2.

[0031] To avoid thermal stress damage to the bow-shaped heat exchange tube bundle 5 caused by the expansion and contraction of the pipeline due to temperature changes during startup and shutdown, during the installation of the bow-shaped heat exchange tube bundle 5, pre-cold drawing is carried out so that the swing amplitudes under the maximum tensile stress and compressive stress are equal:

[0032] ΔL / 2 = ΔL1 + ΔL2

[0033] ΔL1 = ΔL2

[0034] Where: ΔL — the compensation length of the bow-shaped heat exchange tube, in mm

[0035] ΔL1 — the swing amplitude of each vertical arm of the bow-shaped heat exchange tube under the action of the maximum tensile stress, in mm

[0036] ΔL2 — the swing amplitude of each vertical arm of the bow-shaped tube under the action of the maximum compressive stress, in mm

[0037] Manholes 31 are provided on the tower body 4 in the opening direction of the horizontal section of the bow-shaped heat exchange tube bundle 5. These manholes 31 are used for entering and exiting the tower body 4, and adsorption packing is filled at the corresponding positions. The vertical space formed inside the tower body between the lower head 2 and the upper head 9 is the main adsorption zone 6 for raw gas adsorption and impurity removal and temperature-rising desorption. The adsorption packing filled here undertakes the main adsorption and separation function. The adsorption zone 6 is filled with adsorption packing, including but not limited to activated carbon, silica gel, molecular sieve, etc. according to the gas purification requirements.

[0038] Further, the heat exchange type temperature swing adsorption tower further includes an upper distributor 7, an inter-tube gas distributor 20, and a lower distributor 3. The upper distributor 7 is arranged inside the connection between the upper head 9 and the upper end of the tower body 10. The lower distributor 3 is arranged inside the connection between the lower head 2 and the lower end of the tower body 4. The inter-tube gas distributor 20 is arranged in the middle inside the tower body 4.

[0039] Further, the inlet 21 and the outlet 22 of the heat exchange main pipe extend outside the tower body 4.

[0040] Further, an outlet filter 8 is arranged inside the upper port 10.

[0041] Further, the upper distributor 7 corresponds to the upper port 10 of the adsorption tower and is in a flat plate shape. The flat plate distributor is one to multiple layers of orifice plates. To prevent the fluidization of the adsorption bed, the orifice plates adopt a structure of ceramic balls or mechanical pressing.

[0042] Further, when the diameter of the adsorption tower of the lower distributor 3 is ≤ 2m, it adopts a flat plate shape.

[0043] Further, when the diameter of the adsorption tower of the lower distributor 3 is > 2m, it adopts a frustum shape, and gas holes are opened at the top and side of the frustum.

[0044] The above is only the preferred specific implementation manner of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present invention, according to the technical solution and its concept of the present invention, makes equivalent substitutions or changes, and all should be covered within the protection scope of the present invention.

[0045] The following embodiments are implemented on the premise of the technical solution of the present utility model, and detailed implementation manners and specific operation processes are given. However, the protection scope of the present utility model is not limited to the following embodiments. The methods used in the following embodiments are all conventional methods unless otherwise specified.

[0046]

Embodiment

[0047] As Figures 5-6 shown, the actual volume flow rate of the coke oven gas is 12716 m 3 / h. The calculated tower diameter is 3.6 m. Since the tower diameter > 2 m, the lower distributor 3 is selected as a conical distributor, which has the advantages of small void volume, strong supporting ability, and a large amount of adsorbent in the head. Gas holes are opened at the top and side of the cone. According to the above-mentioned impurity content of the coke oven gas and the adsorption time of 6 h, the total impurity adsorption amount is 8.5 t. If the adsorption capacity is 40% and the surplus coefficient is taken as 1.25, the total filling amount of the adsorbent is calculated to be 27 t. If the bulk density is considered as 520 kg / m 3 When considered, the required packing volume is 52 m 3 , and the filling height is determined to be 5 m according to the tower diameter, so as to determine the distance between the inlet 21 and the outlet 22 of the heat exchange main pipe as 5 m;

[0048] Obtained by H = a·B, the horizontal section length of the bow-shaped heat exchange tube bundle 5 is 1 m, the vertical section length is 1 m, and there are four horizontal openings. There are four manholes 31 arranged on both sides of the tower body.

[0049] Starting from the bottommost manhole 31, the adsorption packing is filled into the adsorption zone 6 in the tower body 4. After reaching the position of the manhole 31 and being compacted, the adsorption packing is continuously filled upward through the manhole 31 until the entire adsorption zone 6 is filled with the adsorption packing.

[0050] The raw material gas enters from the lower port 1 of the adsorption tower. After the raw material gas passes through the upper distributor 7, the inter-tube gas distributor 20 and the lower distributor 3 to equalize the pressure and slow down the rising speed, it slowly passes through the adsorption zone 6. The adsorption packing in the adsorption zone 6 adsorbs and removes tar, benzene, naphthalene, hydrogen sulfide, ammonia, hydrogen cyanide, and some organic sulfur in the raw material gas, and the purified raw material gas is output from the upper port 10.

[0051] When the adsorption packing reaches the adsorption limit, the desorbing gas enters from the upper port 10, and the heat exchange medium is introduced through the bow-shaped heat exchange tube bundle 5 to heat the desorbing gas and the adsorption packing, so that the adsorption packing is desorbed and regenerated. The impurity gas and the desorbing gas are discharged together from the lower port 1. The manhole is arranged at the horizontal opening position of the bow-shaped heat exchange tube bundle 5, which is convenient for loading the adsorbent, can supplement the adsorption packing at any time, increases the service life of the adsorption tower, and reduces the operation cost.

Claims

1. A heat exchange type variable temperature 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, and the upper port, the upper head, the lower head and the lower port are sequentially connected from top to bottom. It is characterized in that, The vertical space inside the tower body is the adsorption zone, where an arc-shaped heat exchange tube bundle is arranged. The arc-shaped heat exchange tube bundle consists of a vertical and horizontal heat exchange tube network composed of multiple groups of "straight tubes" arranged in a "bow" shape. The arc-shaped heat exchange tube bundle is connected to the inlet of the heat exchange main pipe at the upper part of the tower body and to the outlet of the heat exchange main pipe at the lower part of the tower body. A manhole is provided on the tower body in the opening direction of the horizontal section of the arc-shaped heat exchange tube bundle.

2. The heat exchange type variable temperature adsorption tower according to claim 1, characterized in that, 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 arranged inside the connection between the upper head and the upper end of the tower body, the lower distributor is arranged inside the connection between the lower head and the lower end of the tower body, and the inter-tube gas distributor is arranged in the middle inside the tower body.

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

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

5. The heat exchange type variable temperature adsorption tower according to claim 2, characterized in that, The upper distributor is of a flat plate shape and adopts a structure with ceramic balls or mechanical pressing.

6. The heat exchange type variable temperature adsorption tower according to claim 2, characterized in that, When the diameter of the adsorption tower is ≤ 2m, the lower distributor is of a flat plate shape.

7. The heat exchange type variable temperature adsorption tower according to claim 2, characterized in that, When the diameter of the adsorption tower is > 2m, the lower distributor is of a frustum shape, and gas holes are opened at the top and side of the frustum.

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