Desulfurization and decarburization rotating bed layer and rotating tower using same

Abstract

The invention discloses a desulfurization and decarburization rotating bed layer, which is arranged in the same tower, is used for a desulfurization and decarburization process of flue gas running from bottom to top, and comprises a plurality of layers of support grids which are in clearance fit with the inner wall of the tower, the lower bed layer forms a desulfurization bed layer, and the upper bed layer forms a decarburization bed layer; the multiple layers of supporting grids are fixedly connected with a rotating shaft; in the rotation process of the bed layer, the liquid absorbent which runs from top to bottom and is used for desulfurization and decarbonization is smashed into fine fog drops, and the fog drops form a thin surface with a certain thickness under the action of rotation inertia. The invention also discloses a rotating tower applying the rotating bed layer. According to the invention, desulfurization and decarbonization are integrated in one tower, and the rotatable grating is used as a bed layer, so that gas-liquid mass transfer can be enhanced, desulfurization, decarbonization and dust removal are realized, and good mechanical properties and anti-scaling and anti-blocking functions are also realized.

Description

Technical Field

[0001] The present invention relates to the technical field of industrial waste gas treatment and gas-liquid mass transfer, in particular to a desulfurization and decarbonization rotating bed layer and a rotating tower using the bed layer. Background Art

[0002] GB31570-2015, "Petroleum Refining Industry Pollutant Emission Standard," stipulates limits for atmospheric pollutant emissions. Special limits apply in areas with high land development density and low environmental carrying capacity, requiring special protective measures. In some areas, the requirements are even stricter.

[0003] Currently, organic amine absorption technology is relatively mature, but it is limited by high operating costs. For example, Chinese patent application CN115738663A discloses an ammonia-based desulfurization and decarbonization device and method for producing long-acting ammonium bicarbonate. The device includes a desulfurization unit, a decarbonization unit, an ammonia supply unit, an ammonium bicarbonate treatment unit, and an additive supply unit. The ammonia additive supply unit is connected to the ammonium bicarbonate treatment unit. Ammonia absorbent and additives are added to the ammonium bicarbonate treatment unit, and the mother liquor is refluxed to the desulfurization and decarbonization units to produce long-acting ammonium bicarbonate.

[0004] Although this type of existing equipment can efficiently decarbonize and produce long-lasting ammonium bicarbonate fertilizer at the same time, the removal efficiency is low due to the limited gas-liquid mass transfer effect of traditional tower equipment. The desulfurization unit and decarbonization unit of traditional tower equipment are generally split-type designs, desulfurizing first and then decarbonizing. The desulfurization unit and decarbonization unit equipment are large in size and require a large floor space. In addition, the dust and particulate matter contained in the flue gas will cause blockage of the bed layer in the device and increase the pressure drop over a long period of operation, affecting normal production.

[0005] Therefore, there is an urgent need for a desulfurization and decarbonization rotating bed and a rotating tower using the bed, which can not only enhance gas-liquid mass transfer, but also have good mechanical properties and anti-scaling and clogging functions while desulfurizing, decarbonizing and removing dust.

[0006] The information disclosed in this background technology section is only intended to enhance understanding of the overall background of the invention and should not be regarded as an admission or any form of suggestion that the information constitutes the prior art already known to a person skilled in the art. Summary of the Invention

[0007] The purpose of the present invention is to provide a rotating bed for desulfurization and decarbonization and a rotating tower using the bed, which can concentrate desulfurization and decarbonization in one tower. By using a rotatable grid as a bed, it can not only enhance gas-liquid mass transfer, but also have good mechanical properties and anti-scaling and clogging functions while desulfurizing, decarbonizing and removing dust.

[0008] To achieve the above-mentioned purpose, according to the first aspect of the present invention, the present invention provides a desulfurization and decarbonization rotating bed layer, which is arranged in the same tower and is used for a desulfurization and decarbonization process in which flue gas runs from bottom to top. The desulfurization and decarbonization process comprises at least: a supporting grid, which is multi-layered and fits in with the inner wall of the tower, the lower bed layer constitutes a desulfurization bed layer, and the upper bed layer constitutes a decarbonization bed layer; the multi-layer supporting grid is fixedly connected to a rotating shaft; during the rotation of the bed layer, the liquid absorbent for desulfurization and decarbonization running from top to bottom is broken into fine droplets, and the droplets form a thin surface of a certain thickness under the action of rotational inertia.

[0009] Furthermore, in the above technical solution, the hollow area of ​​the supporting grille may be provided with a screen for removing dust and particulate matter from the flue gas.

[0010] Furthermore, in the above technical solution, the upper portion of the support grid may be provided with evenly spaced branch portions, which are integrally formed with the support grid and are used to increase the impact surface in a local area and form a local droplet thin surface.

[0011] Furthermore, in the above technical solution, the branch portion can be designed as a conical or curved surface structure. When the branch portion is a conical surface, the conical surface can be arranged to tilt upward from the inside to the outside or tilt downward from the inside to the outside. When the branch portion is a curved surface, the curved surface can adopt a single curved surface or a double curved surface structure.

[0012] Furthermore, in the above technical solution, the screen can be made of stainless steel wedge wire, with the small side of the wedge wire facing upward and the large side facing downward, which is used to further cut the droplets while intercepting dust and particulate matter in the flue gas.

[0013] Furthermore, in the above technical solution, the desulfurization bed layer can be set to 1-3 layers, and the decarbonization bed layer can be set to 2-4 layers.

[0014] Furthermore, in the above technical solution, a collection trough can be provided at the bottom edge of the support grid, at the bottom of the desulfurization bed layer, to collect some of the liquid absorbent that is thrown toward the tower wall and recycle it outside the tower. The collection trough can be designed as an overflow structure, consisting of a horizontal section near the tower wall and an inclined section with its upper edge resting against the lower edge of the support grid. When the liquid level in the collection trough rises above the upper edge of the inclined section, the absorbent overflows to the tower bottom.

[0015] According to the second aspect of the present invention, there is provided a rotating tower, which uses the desulfurization and decarbonization rotating bed described in any one of the above items. In the rotating tower, the rotating shaft for driving the supporting grid to rotate is driven by a motor arranged at the bottom outside the tower.

[0016] Furthermore, in the above technical solution, a liquid absorbent inlet can be provided on the wall of the rotating tower and above each bed layer; and a flue gas inlet is provided on the lower wall of the rotating tower.

[0017] Furthermore, in the above technical solution, a first absorbent outlet may be provided at the liquid absorbent collection tank, and a second absorbent outlet may be provided at the bottom of the rotating tower. Both the first and second absorbent outlets may be connected to a collection tank outside the tower, which separates the dust particles and pumps them to the liquid absorbent inlet for recycling.

[0018] Furthermore, in the above technical solution, the liquid absorbent is an alkaline solution or an amine solution that can desulfurize and decarbonize, and the mass concentration of the solution is 5-40%. The amine solution is preferably N-methyldiethanolamine.

[0019] Compared with the prior art, the present invention has the following beneficial effects:

[0020] 1) The desulfurization and decarbonization rotating bed design of the present invention can complete desulfurization and decarbonization in sequence in the same tower, thereby effectively reducing the volume of the equipment; the flue gas runs from bottom to top and meets the liquid absorbent running from top to bottom. Under the action of the rotating bed, the liquid absorbent hits the bed from top to bottom, and the support grid of the bed breaks the liquid into fine droplets. The droplets form a thin surface of a certain thickness due to the rotational inertia, which can carry out gas-liquid mass transfer with the flue gas from bottom to top, effectively extending the residence time of the flue gas in the rotating tower, improving the gas-liquid mass transfer effect between the flue gas and the liquid absorbent, and thus effectively improving the absorption rate of SO2 and CO2; at the same time, the bed constructed by the rigid support grid has good mechanical properties and anti-scaling and clogging functions, which can effectively extend the operating life of the device;

[0021] 2) The present invention uses a screen design that allows excess liquid absorbent to pass through the screen into the next rigid bed layer for absorption reaction, thereby improving the utilization rate of the absorbent and preventing liquid from submerging the bed layer and causing flooding;

[0022] 3) The present invention utilizes the structure and orientation of the wedge wires of the screen, with the small edges facing upward to obtain more sharp edges. The absorbent droplets flowing from top to bottom can be further cut into smaller droplets by the edges of the wedge wires, thereby increasing the contact area between the absorbent and the flue gas in the next bed layer and further improving the gas-liquid mass transfer efficiency. The large edges of the wedge wires facing downward can reduce the distance between each wedge wire, which is more conducive to intercepting dust and particulate matter in the flue gas during the flue gas flow from bottom to top.

[0023] 4) The branches of the present invention are integrally formed with the support grid, which can be used to increase the impact surface in a local area and form a localized droplet thin surface. Because the branches adopt a planar structure, the impact area of ​​the droplets can be increased locally, better breaking up the droplets;

[0024] 5) The branch portion of the present invention can be designed as a conical structure. The "inverted cone" structure can temporarily retain a portion of the liquid absorbent, so that this portion of the absorbent can have a longer residence time in the bed layer. This portion of the absorbent can be thrown out in a surface shape under the rotation of the bed layer, so as to better contact with the rising flue gas; adopting the "umbrella-shaped" structural design, when the bed layer rotates, the tip can not only effectively cut the droplets, but also obtain a thin surface of droplets locally, and also obtain a better gas-liquid mass transfer effect; designing the branch portion as an arc surface can further increase the impact area and improve the gas-liquid mass transfer effect.

[0025] 6) The rotating bed used in the present invention is highly flexible in operation and can be easily assembled into a skid-mounted device for easy mobility. Furthermore, the rotating bed can adapt to the needs of various working conditions and is particularly suitable for plant construction or renovation of old plants under space-constrained conditions, with excellent industrial application prospects. Due to the use of a highly efficient integrated desulfurization and decarbonization process, it can adapt to the needs of various working conditions. The decarbonization absorbent and the desulfurization absorbent can share one of the amine solutions, achieving simultaneous removal of CO2 and SO2, avoiding problems such as equipment scaling and clogging caused by excessive absorbent input. Furthermore, the amine solution absorbent is regenerable, effectively reducing the cost of the absorbent.

[0026] 7) Using the device of the present invention, experiments have shown that the sulfur dioxide removal rate is 95%, the carbon dioxide removal rate is 80%, the absorbent utilization rate is 80%, the overall equipment footprint is reduced by 50%, and the device can operate continuously for more than one year.

[0027] The above description is only an overview of the technical solution of the present invention. In order to more clearly understand the technical means of the present invention and to implement it according to the contents of the specification, and to make the above and other purposes, technical features and advantages of the present invention easier to understand, one or more preferred embodiments are listed below and described in detail with reference to the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 It is a schematic diagram of the internal structure of the rotating tower of the present invention (showing the desulfurization and decarbonization rotating bed layer).

[0029] Figure 2 It is a schematic diagram of the support grid structure of each rotating bed layer of the present invention (showing the screen constructed of part of the wedge wire, and not showing the branches on the support grid).

[0030] Figure 3 Schematic diagram of the structure of the absorbent collecting tank of the present invention (support grid is not shown).

[0031] Figure 4 It is a schematic diagram of the relative position relationship between the absorbent collecting tank and the supporting grid of the present invention.

[0032] Figure 5Schematic diagram of the arrangement of the wedge wire of the present invention.

[0033] Figure 6-A It is a schematic diagram of the first embodiment of the branch portion of the present invention.

[0034] Figure 6-B It is a schematic diagram of a second embodiment of the branch portion of the present invention.

[0035] Figure 6-C It is a schematic diagram of a third embodiment of the branch portion of the present invention.

[0036] Figure 6-D It is a schematic diagram of a fourth embodiment of the branch portion of the present invention.

[0037] Description of main reference numerals:

[0038] 1-desulfurization and decarbonization rotating bed, 11-single bed, 11A-first bed, 11B-second bed, 11C-third bed, 111-support grid, 112-wedge wire, 113-branch portion, 113A-first branch, 113B-second branch, 113C-third branch, 113D-fourth branch, 12-rotating axis, 13-collecting tank, 131-horizontal section, 132-inclined section;

[0039] 100 - rotating tower, 101 - absorbent inlet, 102 - flue gas inlet, 103 - first absorbent outlet, 104 - second absorbent inlet, 105 - collection tank, 106 - circulation pump, 107 - dust particle collector, 108 - motor. DETAILED DESCRIPTION

[0040] The specific embodiments of the present invention are described in detail below with reference to the accompanying drawings, but it should be understood that the protection scope of the present invention is not limited by the specific embodiments.

[0041] Unless expressly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising” will be understood to include the stated elements or components but not to exclude other elements or components.

[0042] In this document, for ease of description, spatially relative terms such as "below," "beneath," "down," "above," "above," etc. may be used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that the spatially relative terms are intended to encompass different orientations of an object in use or operation in addition to the orientation depicted in the drawings. For example, if the object in the figure is turned over, the element described as being "below" or "below" other elements or features will be oriented "above" the element or feature. Therefore, the exemplary term "below" can include both below and above directions. Objects may also have other orientations (rotated 90 degrees or other orientations) and the spatially relative terms used herein should be interpreted accordingly.

[0043] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit specific positions or relative relationships. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable with each other.

[0044] The inventors have discovered that desulfurization and decarbonization can be performed simultaneously using either alkaline or amine solutions. To address the issues of high viscosity and poor fluidity caused by low amine solution temperature, rotating bed technology can effectively improve gas-liquid mass transfer efficiency and reduce equipment size. Compared to other process intensification reactors, rotating beds offer greater operational flexibility and can be easily assembled into skid-mounted equipment for easy mobility. Furthermore, rotating beds can adapt to a variety of operating conditions, making them particularly suitable for plant construction or renovation in space-constrained locations. Experimental studies have shown that they have excellent industrial application prospects.

[0045] like Figure 1 As shown, based on the above research of the inventors, the present invention provides a desulfurization and decarbonization rotating bed 1, which is arranged in the same tower (i.e., a rotating tower 100), and completes the desulfurization and decarbonization processes in the same tower, and can be used for a desulfurization and decarbonization process in which flue gas runs from bottom to top. The desulfurization and decarbonization rotating bed can be provided with two or more bed layers 11, and each bed layer 11 includes at least one supporting grid 111. For a multi-bed setting, the supporting grid 111 is multi-layered and fits with the inner wall of the tower. The lower bed layer (which can be one or more layers) constitutes the desulfurization bed layer, and the upper bed layer (which can also be one or more layers) constitutes the decarbonization bed layer. The multi-layer supporting grid 111 is fixedly connected to a rotating shaft 12. During the rotation of the bed layer, the liquid absorbent for desulfurization and decarbonization running from top to bottom is broken into fine droplets, and the droplets form a thin surface of a certain thickness under the action of the rotation inertia.

[0046] In the desulfurization and decarbonization rotating bed of the present invention, the lower bed serves as a desulfurization bed and the upper bed serves as a decarbonization bed, and desulfurization and decarbonization can be completed in sequence in the same tower, thereby effectively reducing the volume of the equipment; the flue gas runs from bottom to top and meets the liquid absorbent running from top to bottom. Under the action of the rotating bed, the liquid absorbent hits the bed from top to bottom, and the support grid of the bed breaks the liquid into fine droplets. The droplets form a thin surface of a certain thickness due to the rotational inertia, which can carry out gas-liquid mass transfer with the flue gas from bottom to top, effectively extending the residence time of the flue gas in the rotating tower, and improving the gas-liquid mass transfer effect between the flue gas and the liquid absorbent, thereby effectively improving the absorption rate of SO2 and CO2; the bed constructed by the rigid support grid has good mechanical properties and anti-scaling and clogging functions, which can effectively extend the operating life of the device.

[0047] Further Figure 2 、 5 As shown, the hollow area of ​​the support grid 111 is provided with a screen, which can be used to remove dust and particulate matter in the flue gas. Preferably, but not restrictively, the screen can be made of stainless steel wedge wire 112 (materials such as 302, 304, 304L, 316, 316L, etc.), with the small side of the wedge wire 112 facing upward and the large side facing downward. Through such a structure and orientation design, the small side facing upward can obtain more sharp edges, and the absorbent droplets running from top to bottom (refer to Figure 5 The solid arrow direction in the figure) can be further cut into smaller droplets by the edge of the wedge wire, so that the contact area between the absorbent droplets running to the next bed layer and the flue gas is larger, further improving the gas-liquid mass transfer efficiency; the large side of the wedge wire 112 is set downward so that the distance between each wedge wire is smaller, which is more conducive to the bottom-up flue gas (reference Figure 5 During operation (in the direction of the dotted arrow in the figure), dust and particulate matter in the flue gas are intercepted. After being intercepted at the screen, the dust and particulate matter can gradually settle at the bottom of the rotating tower 100 under the influence of their own gravity, the flushing of the liquid absorbent and the rotation of the bed.

[0048] Further Figures 6-A to 6-D As shown, the upper portion of the support grid (i.e., a single bed layer 11) may be provided with evenly spaced branches 113, which are integrally formed with the support grid to increase the impact surface in a local area and form a local droplet thin surface. Preferably, but not restrictively, the branch portion 113 may be a conical or curved surface structure. Further, when the branch portion 113 is a conical surface, the direction of the conical surface may be inclined upward from the inside to the outside (i.e., Figure 6-A The first embodiment shown in FIG. 1 may also be arranged to be tilted downward from the inside to the outside (ie Figure 6-B The second embodiment shown in FIG. 1 ). Since the branch portion adopts a planar structure, the impact area of ​​the droplets can be increased locally, and the droplets can be better dispersed. Figure 6-AIn the first embodiment shown, not only the impact area is increased, but the "inverted cone" structure (i.e., the first branch 113A) can also temporarily retain a portion of the liquid absorbent, allowing this portion of the absorbent to have a longer residence time in the bed. This portion of the absorbent can be ejected in a planar shape under the rotation of the bed, thereby better contacting the rising flue gas. Figure 6-B In the second embodiment shown, due to the "umbrella-shaped" structure (i.e., the second branch 113B) design, when the bed rotates, the tip can not only effectively cut the droplets, but also obtain a thin surface of droplets locally, and also obtain a better gas-liquid mass transfer effect; Figure 6-C and Figure 6-D In the third and fourth embodiments shown, the branch portion is designed as an arc surface, which can be a double-arc surface structure (i.e., the third branch 113C) or a single-arc surface structure (i.e., the fourth branch 113D), which can further increase the impact area and improve the gas-liquid mass transfer effect.

[0049] Further Figure 1 As shown, the desulfurization bed can be set up in 1-3 layers (i.e., the 1-3 layers at the bottom), and the decarbonization bed can be set up in 2-4 layers (i.e., the 2-4 layers at the top). The figure shows three layers of beds, wherein the first bed 11A at the bottom is mainly used for desulfurization, and the second bed 11B and the third bed 11C upwards are mainly used for decarbonization. Figure 1 、 3 4, preferably but not limited to, the bottom layer of the desulfurization bed (i.e. Figure 1 A collection trough 13 is provided at the bottom of the outer edge of the support grid and is used to collect some of the liquid absorbent that is thrown toward the tower wall for recirculation outside the tower. This trough 13 can be designed as an overflow structure, consisting of a horizontal section 131 near the tower wall and an inclined section 132 with its upper edge resting against the lower edge of the support grid. When the liquid level in the trough 13 rises above the upper edge of the inclined section, the absorbent overflows to the tower bottom. This portion of absorbent, which is essentially free of dust and particulate matter, can be directly discharged through the first absorbent outlet 103 for recycling.

[0050] like Figure 1As shown, the present invention also provides a rotating tower 100, which uses the aforementioned desulfurization and decarbonization rotating bed 1, and the rotating shaft 12 for driving the support grid to rotate can be driven by a motor 108 arranged at the bottom outside the tower. A liquid absorbent inlet 101 can be provided on the tower wall of the rotating tower 100 and above each bed; a flue gas inlet 102 is provided on the lower wall of the rotating tower 100. The aforementioned first absorbent outlet 103 is provided at the liquid absorbent collection tank 13, and a second absorbent outlet 104 is provided at the bottom of the rotating tower 100. As mentioned above, the first absorbent outlet 103 can be directly recycled, or the first absorbent outlet 103 and the second absorbent outlet 104 (this outlet needs to be separated and reused because the dust particles are deposited at the bottom and the amount of particles in the absorbent is large) can be connected to the collection tank 105 outside the tower ( Figure 1 As shown), the collection tank 105 can separate the dust particles and pump them to the liquid absorbent inlet 101 through the circulation pump 106 for recycling, and the dust particles are collected by the dust particle collector 107.

[0051] The present invention performs desulfurization and decarbonization within a single rotating tower and utilizes a single absorbent. The liquid absorbent is an alkaline solution or an amine solution capable of both desulfurization and decarbonization. The absorbent may be one, two, or more of the alkaline solution and the amine solution. The alkaline solution may include calcium hydroxide (Ca(OH)2), sodium carbonate (Na2CO3), sodium hydroxide (NaOH), potassium oxide (KOH), ammonium hydroxide (NH4OH), or ammonium bicarbonate (NH4HCO3). The amine solution may include monoethanolamine (MEA), diethanolamine (DEA), piperazine (HPP), triethanolamine (TEA), 2-amino-2-methyl-1-propanol (AMP), diethylenetriamine (DETA), para-diazine (PZ), or N-methyldiethanolamine (MDEA), with N-methyldiethanolamine (MDEA) being preferred. The mass concentration of the solution may range from 5 to 40%.

[0052] Example 1

[0053] A catalytic cracking system adopts the device and process of the present invention, the flue gas flow rate at the denitrification outlet is 120,000 cubic meters per hour, and the sulfur dioxide concentration in the flue gas is 1000 mg / Nm 3 , carbon dioxide concentration is 15%, flow rate is 15m / s, temperature is 200℃, and N-methyldiethanolamine (MDEA) is used as absorbent. The rotating tower is equipped with 3 layers of rigid beds, of which 2 layers are used to remove CO2 and 1 layer is used to remove SO2. The angle between the inclined section and the horizontal section of the collecting tank is 135°. The screen material is 304L stainless steel wedge wire. The branches on the support grid are made of Figure 6-A The first branch structure in .

[0054] The flue gas (200℃) at the denitrification outlet enters the rotating tower, and after desulfurization and decarbonization, it enters the atmosphere through the top outlet of the rotating tower. The MDEA solution enters the absorbent inlet pipe of the rotating tower. The flue gas first completes gas-liquid mass transfer with the MDEA solution in the desulfurization bed (i.e. the bottom layer) to remove sulfur dioxide from the flue gas; the upward flue gas further completes gas-liquid mass transfer with the MDEA solution in the decarbonization bed (i.e. the upper two layers) to remove carbon dioxide from the flue gas; a part of the MDEA solution passes through the collection tank and is regenerated and reused through the first absorbent outlet, and the other part is collected at the bottom of the rotating tower and then drawn out through the second absorbent outlet pipe to separate the solid particles and then regenerated and reused. The regenerated MDEA solution is returned to the rotating tower through the absorbent circulation pump.

[0055] According to calculations, the device of the present invention has a sulfur dioxide removal rate of 95%, a carbon dioxide removal rate of 80%, an absorbent utilization rate of 80%, and a total equipment footprint reduced by 50%. The device can operate continuously for more than one year.

[0056] Comparative Example

[0057] A traditional wet desulfurization unit is equipped with a traditional absorption regeneration tower for decarbonization. The flue gas flow rate at the denitrification outlet is 120,000 cubic meters per hour, and the sulfur dioxide concentration in the flue gas is 1000 mg / Nm 3 , carbon dioxide concentration is 15%, flow rate is 15m / s, temperature is 2000℃, MDEA solution is used as decarbonization absorbent, and sodium hydroxide is used as desulfurization absorbent.

[0058] The flue gas from the denitrification outlet (200°C) directly enters the wet desulfurization tower. After the flue gas is desulfurized (60°C), it enters the carbon capture device and finally leaves the device through the flue gas outlet pipe. After MDEA absorbs carbon dioxide in the absorption tower, it is regenerated in the regeneration tower.

[0059] After calculation, the carbon dioxide removal rate is 60%, the sulfur dioxide removal rate is 90%, the absorbent utilization rate is 60%, the cost of the traditional wet desulfurization and decarbonization overall device is 2.5 times that of Example 1, and the overall process device covers an area of ​​2 times that of Example 1.

[0060] The foregoing descriptions of specific exemplary embodiments of the present invention are for purposes of illustration and description. These descriptions are not intended to limit the invention to the precise form disclosed, and it is apparent that many changes and variations are possible in light of the foregoing teachings. The exemplary embodiments are selected and described for the purpose of explaining the specific principles of the invention and their practical application, thereby enabling those skilled in the art to realize and utilize a variety of exemplary embodiments of the invention and various options and variations. Any simple modifications, equivalent variations, and modifications made to the exemplary embodiments described above are intended to fall within the scope of protection of the present invention.

Claims

1. A desulfurization and decarbonization rotating bed, characterized in that: The desulfurization and decarbonization process for flue gas running from bottom to top is set in the same tower, including: The support grid is arranged in multiple layers and is fitted with a gap between the inner wall of the tower. The lower bed layer constitutes a desulfurization bed layer and the upper bed layer constitutes a decarbonization bed layer. The multi-layer support grid is fixedly connected to a rotating shaft. During the rotation of the bed layer, the liquid absorbent for desulfurization and decarbonization running from top to bottom is broken into fine droplets, and the droplets form a thin surface of a certain thickness under the action of rotational inertia.

2. The desulfurization and decarbonization rotating bed according to claim 1, characterized in that: The hollow area of ​​the support grid is provided with a screen for removing dust and particulate matter in the flue gas.

3. The desulfurization and decarbonization rotating bed according to claim 1, characterized in that: The upper part of the support grid is provided with evenly spaced branch portions, which are integrally formed with the support grid and are used to increase the impact surface in a local area and form a local droplet thin surface.

4. The desulfurization and decarbonization rotating bed according to claim 3, characterized in that: The branch portion is a conical or arc surface structure.

5. The desulfurization and decarbonization rotating bed according to claim 4, characterized in that: When the branch portion is a conical surface, the conical surface is arranged to be inclined upward from the inside to the outside or inclined downward from the inside to the outside.

6. The desulfurization and decarbonization rotating bed according to claim 4, characterized in that: When the branch portion is a curved surface, the curved surface is a single curved surface or a double curved surface structure.

7. The desulfurization and decarbonization rotating bed according to claim 2, characterized in that: The screen is made of stainless steel wedge wire, with the small side of the wedge wire facing upward and the large side facing downward, and is used to further cut the mist droplets while intercepting dust and particulate matter in the flue gas.

8. The desulfurization and decarbonization rotating bed according to claim 1, characterized in that: The desulfurization bed layer is provided with 1-3 layers, and the decarbonization bed layer is provided with 2-4 layers.

9. The desulfurization and decarbonization rotating bed according to claim 8, characterized in that: A collecting trough is provided at the bottom of the outer edge of the supporting grid at the lowest layer of the desulfurization bed for collecting part of the liquid absorbent thrown toward the tower wall and circulating it outside the tower for regeneration.

10. The desulfurization and decarbonization rotating bed according to claim 9, characterized in that: The collecting tank is an overflow structure, consisting of a horizontal section close to the tower wall and an inclined section with its upper edge resting against the lower edge of the support grid. When the liquid level in the collecting tank is higher than the upper edge of the inclined section, the absorbent overflows to the bottom of the tower.

11. A rotating tower, characterized in that: The desulfurization and decarbonization rotating bed as claimed in any one of claims 1 to 10 is used, and the rotating shaft for driving the supporting grid to rotate is driven by a motor arranged at the bottom outside the tower.

12. The rotating tower according to claim 11, characterized in that A liquid absorbent inlet is arranged on the tower wall of the rotating tower and above each bed layer; and a flue gas inlet is arranged on the lower wall of the rotating tower.

13. The rotating tower according to claim 12, characterized in that: A first absorbent outlet is provided at the liquid absorbent collection tank, and a second absorbent outlet is provided at the bottom of the rotating tower. Both the first and second absorbent outlets are connected to a collection tank outside the tower, which separates the dust particles and pumps them to the liquid absorbent inlet for recycling.

14. The rotating tower according to claim 12, wherein: The liquid absorbent is an alkali solution or an amine solution which can desulfurize and decarbonize, and the mass concentration of the solution is 5-40%.

15. The rotating tower according to claim 14, characterized in that The amine liquid is N-methyldiethanolamine.

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