Carbon capture unit and hypergravity rotating bed applying the same

Abstract

The application discloses a carbon capture unit and a supergravity rotating bed applying the unit, the carbon capture unit is arranged in a spherical reactor and comprises a rotating shaft vertically penetrating the spherical reactor, and tree-shaped baffles which are integrally tree-shaped and are arranged in layers in the circumferential direction of the rotating shaft, the number of baffles in each layer is multiple and the baffles are uniformly arranged at intervals, and the baffles of adjacent layers are arranged at a deviated angle in the radial direction. The baffles are fixedly connected with the rotating shaft through connecting rods, and the length of the connecting rod of the lower baffle is greater than that of the upper baffle. In the rotating process of the rotating shaft, liquid for carbon capture impacts the baffles from top to bottom, the baffles break the liquid into fine droplets and make the droplets spiral downward, and the downward droplets perform gas-liquid mass transfer with flue gas rising from bottom to top. The supergravity rotating bed further comprises a baffling unit. While ensuring the flue gas treatment capacity, the application can effectively increase the gas-liquid residence time, improve the mass transfer effect, has high energy utilization rate, and can effectively prolong the operation time of the device.

Description

Technical Field

[0001] This invention relates to the field of gas-liquid mass transfer technology, and in particular to a carbon capture unit and a high-gravity rotating bed using the unit. Background Technology

[0002] Carbon dioxide is one of the major greenhouse gases, and its large-scale emissions have had a serious impact on the global climate and environment. Therefore, there is an urgent need to develop economical and effective carbon capture technologies.

[0003] Chemical absorption is the most widely used carbon capture technology. Currently, absorption methods are mostly carried out in traditional tower equipment (such as packed towers and plate towers), achieving gas-liquid contact and mass transfer under the influence of Earth's gravity. However, due to the weak gravitational field, the liquid film flows slowly, resulting in a small effective contact area per unit volume and a low volumetric mass transfer coefficient controlled by the liquid film. This leads to such equipment being bulky, with low space utilization and low production efficiency. Only by strengthening the gravitational field can the inherent defects of traditional tower equipment be overcome. Therefore, the development of novel hypergravity devices and processes has attracted the attention and favor of researchers both domestically and internationally.

[0004] Carbon capture using hypergravity technology leverages high-speed rotation to generate a gravitational field of 10–1000g, significantly enhancing gas-liquid mass transfer during CO2 capture and improving CO2 capture efficiency. Furthermore, the highly efficient mass transfer of hypergravity reactors allows for smaller equipment size, reduced footprint, and lower investment costs. Moreover, the flexible operation and easy relocation of hypergravity reactors are far superior to traditional tower equipment.

[0005] For example, Chinese patent application CN112206698A discloses a baffle-type high-gravity rotary bed with an integrally rotating rotor, including a shell and a rotor disposed within the shell. A gas outlet pipe is provided in the middle of the top surface of the shell, and a liquid inlet pipe and a liquid outlet pipe are respectively provided on the top and bottom surfaces of the shell at positions off-center. A gas inlet pipe is provided in the lower part of the side wall of the shell. The lower end of the gas outlet pipe is connected to a trumpet-shaped liquid distributor, which extends downward into the rotor. The rotor includes an upper rotating disk and a lower rotating disk, which rotate circumferentially synchronously with the rotating shaft. The rotating shaft passes upward into the shell from the lower end of the shell and is sealed and rotatably connected to the shell. The bottom surface of the upper rotating disk is provided with several first baffle rings of different diameters, and the top surface of the lower rotating disk is provided with several second baffle rings of different diameters, with gaps between adjacent second baffle rings to accommodate the first baffle rings. The first and second baffle rings are nested and staggered. Although this scheme occupies less space, it suffers from drawbacks such as high pressure drop and high power consumption due to the low gas-liquid throughput and short gas-liquid residence time of the rotating bed in the supergravity reactor. Its low energy utilization rate makes it difficult to achieve long-term operation, which limits its application in fields involving solid phases or high-viscosity fluids, such as chemical engineering and materials preparation.

[0006] Therefore, there is an urgent need for a carbon capture unit and a high-gravity rotating bed that uses this unit, which can not only ensure the flue gas treatment capacity, but also effectively increase the gas-liquid residence time and improve the mass transfer effect.

[0007] The information disclosed in this background section is intended only to enhance the understanding of the overall background of the invention and should not be construed as an admission or in any way implying that the information constitutes prior art known to those skilled in the art. Summary of the Invention

[0008] The purpose of this invention is to provide a carbon capture unit and a high-gravity rotating bed using the unit, which can effectively increase the gas-liquid residence time and improve the mass transfer effect while ensuring the flue gas treatment capacity.

[0009] Another objective of this invention is to provide a supergravity rotating bed that not only has high energy utilization but also effectively extends the operating time of the device.

[0010] To achieve the above objectives, according to a first aspect of the present invention, a carbon capture unit is provided, disposed in a spherical reactor, comprising: a rotating shaft vertically inserted into the spherical reactor; tree-shaped baffles, which are generally tree-shaped and arranged in layers along the circumference of the rotating shaft, each layer having multiple baffles evenly spaced, and adjacent layers of baffles having a radial offset angle; the baffles are fixedly connected to the rotating shaft by connecting rods, the connecting rod length of the lower layer baffle being greater than the connecting rod length of the upper layer baffle; during the rotation of the rotating shaft, the liquid used for carbon capture impacts the baffles from top to bottom, the baffles break the liquid into fine droplets and cause the droplets to descend spirally, while simultaneously undergoing gas-liquid mass transfer with the flue gas rising from bottom to top.

[0011] Furthermore, in the above technical solution, each baffle has an inclination angle that satisfies the requirement of perpendicular impact with the liquid; the liquid comes from a liquid distributor installed at the top of the spherical reactor.

[0012] Furthermore, in the above technical solution, the tilt angle of the baffle can be set to decrease layer by layer from top to bottom.

[0013] Furthermore, in the above technical solution, the uppermost baffle is positioned to match the height of the liquid distributor; the lowermost baffle is positioned close to the inner wall of the spherical reactor.

[0014] Furthermore, in the above technical solution, the cross-section of the connecting rod can be flat, with one end fixedly connected to the baffle and the other end fixedly connected to the rotating shaft.

[0015] Furthermore, in the above technical solution, the baffles can be set in 5 to 10 layers, with each layer having an offset angle of 5° to 15°; and each layer has 4 baffles.

[0016] According to a second aspect of the present invention, the present invention provides a supergravity rotating bed, including the aforementioned carbon capture unit.

[0017] Furthermore, in the above technical solution, the supergravity rotating bed also includes: a baffle unit, which is located below the carbon capture unit and at least part of it rotates with the rotating shaft, for receiving liquid from the carbon capture unit after gas-liquid mass transfer and flue gas from the bottom of the spherical reactor, and performing secondary gas-liquid mass transfer through the countercurrent of liquid and flue gas and the baffle effect.

[0018] Furthermore, in the above technical solution, the baffle unit includes: a rotating disk, which is fixedly connected to the rotating shaft, with multiple rings of baffles extending downward from the disk surface, each ring containing multiple baffles that are evenly spaced; and a stationary disk, which is fixedly connected to the wall of the spherical reactor, with multiple baffle rings extending upward from the disk surface, the baffle rings being staggered from the baffles of the corresponding rings; the liquid entering from the outer edge of the rotating disk and the flue gas entering from the inner edge of the stationary disk form countercurrent and baffle flow, thereby realizing the secondary gas-liquid mass transfer.

[0019] Furthermore, in the above technical solution, the number of baffles is the same for each revolution of the rotating disk.

[0020] Furthermore, in the above technical solution, the baffles on each ring of the rotating disk are concentrically installed, the total number of baffle rings is 5 to 15, and the baffle spacing is an integer multiple of 50 mm; the baffle rings on the stationary disk are spaced at an integer multiple of 50 mm, and the distance between the baffle rings and the baffles is an integer multiple of 25 mm; multiple rectangular liquid outlet holes are evenly distributed on the baffle rings.

[0021] Furthermore, in the above technical solution, the baffle unit may include a rotating disk and a stationary disk spaced apart along the axial direction of the rotating shaft. The rotating disk is fixedly connected to the rotating shaft, and the stationary disk is fixedly connected to the wall of the spherical reactor. The liquid running from top to bottom and the flue gas running from bottom to top form countercurrent and baffle in the baffle unit to realize secondary gas-liquid mass transfer.

[0022] Furthermore, in the above technical solution, a gas-liquid distribution plate may be provided below the baffle unit, and the gas-liquid distribution plate is fixedly installed on the wall of the spherical reactor; the gas-liquid distribution plate is sleeved on the rotating shaft and is fitted with the rotating shaft with a clearance, and a liquid overflow hole is provided near the rotating shaft, and ventilation holes are evenly spaced on the gas-liquid distribution plate.

[0023] Furthermore, in the above technical solution, the flue gas inlet of the spherical reactor can be located at the bottom; the flue gas inlet is connected to an inlet pipeline, and an induced draft vane is installed in the inlet pipeline to convert the rotational mechanical energy of the induced draft vane into electrical energy to provide energy for the liquid inlet pump and the liquid outlet pump.

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

[0025] 1) This invention employs a tree-shaped carbon capture unit composed of a rotatable baffle and connecting rods, making the baffle essentially perpendicular to the direction of liquid descent. During rotation, the liquid can be broken into finer droplets, effectively increasing the overall mass transfer rate. Simultaneously, the baffle can change the liquid flow direction. With the overall tree-shaped structure, the droplets descend in a spiral after impact, increasing the droplet travel distance and effectively increasing the gas-liquid contact time, thereby further improving the carbon dioxide absorption effect.

[0026] 2) In the tree-shaped carbon capture unit of the present invention, the baffles of adjacent layers are offset in the radial direction, and the connecting rod length of the lower baffle is greater than that of the upper baffle, so that the baffle can accept the impact of liquid from different directions, reducing the possibility of liquid falling directly. In the state of overall rotation, it is more conducive to the spiral descent of droplets.

[0027] 3) The carbon capture unit of the present invention has a tree-like structure, and the length of each layer of connecting rods is not the same. The length increases from top to bottom. This can satisfy the spiral descent of droplets and ensure the amount of flue gas that can be treated. At the same time, it can make full use of the internal space of the spherical reactor and minimize the impact of liquid entering from the nozzle falling directly into the lower space.

[0028] 4) Carbon capture is performed by combining a dendritic carbon capture unit and a baffle unit as described in the first embodiment. After the first gas-liquid mass transfer is completed in the dendritic carbon capture unit, the liquid enters the baffle unit for a second gas-liquid mass transfer. The droplets collide with the baffle plate of the rotating disk of the baffle unit, causing the droplets to be broken into a large number of smaller droplets. At the same time, during the rotation of the rotating disk, the side of the baffle plate can also cut the droplets, forming a shearing effect on the droplets. The contact area between the two phases increases, enhancing the mass transfer effect and further improving the gas-liquid mass transfer rate of the high gravity rotating bed.

[0029] 5) By combining the dendritic carbon capture unit of the present invention with the baffle unit of the second embodiment, the rotation of the baffle unit's rotating disk can increase the gas-liquid disturbance in the baffle channel and form eddies locally, which is more conducive to gas-liquid mass transfer.

[0030] 6) The gas-liquid distribution plate below the baffle unit of the present invention can reduce the mist entrainment phenomenon that occurs in the existing rotating bed, extend the service life of the device, and enable long-cycle operation.

[0031] 7) This invention sets up an induced draft vane and an energy converter at the flue gas inlet of the spherical reactor. By effectively utilizing the high flue gas velocity at the inlet, the excess kinetic energy in the flue gas can be converted into electrical energy to provide power for devices such as the liquid inlet pump and outlet pump, reducing the energy loss of the entire flue gas treatment system after desulfurization and denitrification. At the same time, since the flue gas velocity is actively reduced, the residence time of the gas in the baffle unit can be effectively extended, thereby further improving the gas-liquid mass transfer effect of the baffle unit.

[0032] The above description is merely an overview of the technical solution of the present invention. In order to better 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 objects, 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. Attached Figure Description

[0033] Figure 1 This is a schematic diagram of the internal supergravity rotating bed of the spherical reactor of the present invention (showing the first embodiment of the carbon capture unit and the baffle unit; the solid arrows in the figure indicate the liquid flow direction, and the dashed arrows indicate the flue gas flow direction).

[0034] Figure 2 This is a top view schematic diagram of the carbon capture unit of the present invention in a spherical reactor.

[0035] Figure 3 This is a schematic diagram of the baffle structure in the carbon capture unit of the present invention.

[0036] Figure 4 This is a schematic diagram of the rotating disk structure of the first embodiment of the baffle unit of the present invention.

[0037] Figure 5 This is a schematic diagram of the stationary disk deflector ring structure of the first embodiment of the deflector unit of the present invention.

[0038] Figure 6 This is a top view schematic diagram of the gas-liquid distribution plate of the present invention.

[0039] Figure 7 This is a schematic diagram of the structure of the supergravity rotating bed inside the spherical reactor of the present invention (showing a second embodiment of the carbon capture unit and the baffle unit).

[0040] Figure 8 This is a schematic diagram illustrating the application of the spherical reactor of the present invention.

[0041] Explanation of key figure labels:

[0042] 100-First spherical reactor, 101-Liquid inlet, 102-Gas outlet, 103-Gas inlet, 104-Liquid outlet; 1-Baffle, 10-Connecting rod, 2-Rotating shaft, 3-Baffle unit, 31-First rotating disk, 32-Vertical baffle, 33-First stationary disk, 34-Baffle ring, 340-Rectangular liquid outlet, 4-Gas-liquid distribution plate, 41-Vent hole, 42-Liquid overflow hole;

[0043] 200 - Second spherical reactor, 31A - Second rotating disk, 33A - Second stationary disk;

[0044] 5-Flue gas inlet pipeline, 51-Induced draft vane, 6-Energy converter, 7-Liquid inlet pump (rich liquid), 8-Liquid outlet pump (lean liquid), 9-Wet desulfurization tower, 11-Rich / lean liquid heat exchanger, 12-Regeneration tower, 13-Flue gas heat exchanger, 14-Denitrification outlet flue gas, 15-Atmosphere, 16-High concentration carbon dioxide product. Detailed Implementation

[0045] The specific embodiments of the present invention will now be described in detail with reference to the accompanying drawings, but it should be understood that the scope of protection of the present invention is not limited to the specific embodiments.

[0046] Unless otherwise expressly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "comprises" shall be understood to include the stated elements or components without excluding other elements or other components.

[0047] In this document, for ease of description, spatial relative terms such as “below,” “under,” “down,” “above,” “above,” “upper,” etc., are used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that spatial relative terms are intended to encompass different orientations of an object in use or operation, in addition to those depicted in the figures. For example, if an object in the figure is flipped, an element described as “below” or “under” another element or feature would be oriented “above” that element or feature. Thus, the exemplary term “below” can encompass both the downward and upward orientations. An object may also have other orientations (rotated 90 degrees or other orientations), and the spatial relative terms used herein should be interpreted accordingly.

[0048] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.

[0049] like Figure 1As shown, this invention provides a carbon capture unit, which is installed in a first spherical reactor 100. This unit can be used to capture carbon dioxide in flue gas after desulfurization and denitrification. It can be used alone or in combination with other types of carbon capture facilities. It includes: tree-shaped baffles and a rotating shaft 2. The rotating shaft 2 is vertically inserted into the spherical reactor, and a dynamic seal is provided at the insertion point. The tree-shaped baffles are arranged in a tree shape and layered along the circumference of the rotating shaft 2. Each layer contains multiple baffles 1, evenly spaced, with adjacent layers of baffles 1 offset at a radial angle. The baffles 1 are fixedly connected to the rotating shaft 2 via connecting rods 10, with the connecting rod length of the lower layer baffle being greater than that of the upper layer baffle. The overall structure composed of all the baffles 1 and the corresponding connecting rods 10 is tree-shaped. During the rotation of the shaft 2, the liquid used for carbon capture (i.e., carbon dioxide absorbent) impacts the baffle 1 from top to bottom. The baffle 1 breaks the liquid into fine droplets, which then spiral downwards, simultaneously engaging in gas-liquid mass transfer with the rising flue gas. This invention employs a tree-like carbon capture unit composed of rotatable baffles and connecting rods, ensuring that the baffle 1 is substantially perpendicular to the liquid's downward direction. During rotation, the liquid is broken into even finer droplets, effectively increasing the overall mass transfer rate. Simultaneously, the baffle 1 can alter the liquid flow direction. The overall tree-like structure causes the impacted droplets to spiral downwards, increasing their travel distance and effectively extending the gas-liquid contact time, thereby further enhancing the carbon dioxide absorption effect. Adjacent layers of baffle 1 are radially offset at an angle (reference). Figure 2 (Top view), and the connecting rod length of the lower baffle is greater than that of the upper baffle, so that the baffle 1 can accept the impact of liquid from different directions, reducing the possibility of liquid falling directly. In the state of overall rotation, it is more conducive to the spiral descent of the droplets.

[0050] Further as Figures 1 to 3 As shown, each baffle 1 has an inclination angle (i.e., tilted inwards, see reference). Figure 3The tilt angle is preferably set to ensure perpendicular impact with the liquid. The liquid originates from a liquid distributor located at the top of the spherical reactor, i.e., a distributor located at the bottom of the inlet 101. The liquid sprayed from the nozzles of this distributor is distributed in an umbrella shape to better impact each layer of baffles 1. Due to the differences in the spray coverage angle and spray stroke of the nozzles, the tilt angle of the baffles can be set to decrease layer by layer from top to bottom. Furthermore, the position of the uppermost baffle is adapted to the height of the liquid distributor, and the position of the lowermost baffle is close to the inner wall of the spherical reactor. Since this invention uses a spherical reactor and a carbon capture unit with an overall tree-like structure, the length of each layer of connecting rods 10 is not the same, increasing layer by layer from top to bottom. This satisfies the spiral descent of droplets, ensuring the amount of flue gas processed, while making full use of the internal space of the spherical reactor and minimizing the possibility of liquid entering from the nozzles falling directly into the lower space without impact. Furthermore, preferably but not limitingly, the cross-section of the connecting rod 10 can be designed to be flat, so that the connecting rod itself can also accept the impact of the liquid, thereby achieving a better atomization effect. One end of the connecting rod 10 is fixedly connected to the baffle 1, and the other end is fixedly connected to the rotating shaft 2, so that each layer of baffle 1 can rotate together with the rotating shaft 2. Specifically, depending on the inner diameter of the spherical reactor, the baffles are preferably arranged in 5 to 10 layers, with an offset angle of 5° to 15° for each layer. Each layer of baffles can be set to 4 in a cross shape (see reference). Figure 2 ).

[0051] Further as Figure 1 As shown, this invention also provides a high-gravity rotating bed, that is, in addition to arranging carbon capture units in a spherical reactor, other carbon capture facilities are also set up. Combined use can further improve the gas-liquid mass transfer effect, thereby obtaining a higher carbon dioxide absorption rate. Specifically, the other carbon capture facilities of this invention can be baffle units. The baffle unit 3 used in this invention is located below the carbon capture unit and at least a portion of it can rotate with the rotating shaft 2. It is used to receive liquid from the carbon capture unit after gas-liquid mass transfer and flue gas from the bottom of the spherical reactor. Secondary gas-liquid mass transfer is achieved through the countercurrent and baffle action of the liquid and flue gas. The fact that a portion of the baffle unit 3 rotates with the rotating shaft means that the baffle unit 3 is configured as a combination of rotating and stationary components. The inventors have found that the baffle units used in the prior art are almost entirely rotating components. In this method, the liquid can only achieve countercurrent and baffle action with the flue gas during operation. Although this can ensure the residence time of the gas and liquid in the baffle unit, the liquid is not easily dynamically sheared during the process, and the atomization effect is not obvious, which significantly hinders the mass transfer between gas and liquid.

[0052] Based on the problems of existing flow deflection units, the flow deflection unit of the first embodiment provided by the present invention includes a rotating disk 31 and a stationary disk 33, as shown in the reference. Figure 1The rotating disk 31 is fixedly connected to the rotating shaft 2, and multiple vertically arranged baffles (i.e., vertical baffles 32) extend downwards from the disk surface. Each ring contains multiple baffles that are evenly spaced. The stationary disk 33 is fixedly connected to the wall of the spherical reactor, and multiple baffle rings 34 extend upwards from the disk surface. The baffle rings 34 and the corresponding baffles 32 are staggered (see reference). Figure 1 The deflector ring 34 differs from the baffle 32 in its arrangement; it is a continuous, ring-like structure. The structure of the deflector ring 34 after unfolding is as follows: Figure 5 As shown, a plurality of rectangular liquid outlet holes 340 are evenly distributed on the baffle ring 34. From the outer edge of the rotating disk 31 (i.e. Figure 1 The liquid entering from the end furthest from the rotating shaft 2 and from the inner edge of the stationary disk 33 (i.e. Figure 1 The flue gas entering from the end near the rotating shaft 2 forms a countercurrent and a deflection, thereby realizing secondary gas-liquid mass transfer (the tree-shaped carbon capture unit realizes primary gas-liquid mass transfer).

[0053] Further reference Figure 4 Preferably, but not limitingly, the number of baffles 32 in each ring of the rotating disk 31 is the same, and they are evenly spaced in the circumferential direction of each ring. The baffles 32 in each ring of the rotating disk 31 are concentrically installed, the total number of rings of baffles can be set to 5 to 15, the baffle spacing is set to 50n (n = 1, 2, 3, ...) mm, and the number of baffles is m (m = 2, 3, 4, ...). Figure 4 In the embodiment, each ring has 6 baffles, and the baffle spacing angle is 360° / m (m = 2, 3, 4, ...). Figure 4 In the embodiment, the interval is 60°. Baffle rings 34 are installed on the stationary disk 33 at intervals of 50n (n = 1, 2, 3, ...) mm, and the distance between the baffle rings 34 and the baffle 32 is 25n (n = 1, 2, 3, ...) mm. The inventors have proven through experiments that the above-mentioned arrangement of the rotating disk and the stationary disk results in a high gas-liquid mass transfer efficiency between the liquid and the flue gas.

[0054] use Figure 1 The spherical reactor shown, along with the dendritic carbon capture unit and the baffle unit of the first embodiment described above, allow liquid to enter the reactor through a nozzle. The liquid collides with baffle 1 at a certain speed, forming finer droplets and changing the liquid's flow direction, causing it to descend in a spiral. Gas encounters the liquid from bottom to top within the reactor, achieving the first gas-liquid mass transfer, resulting in a more complete reaction and higher absorption efficiency. After the first gas-liquid mass transfer, the liquid enters the baffle unit, where droplets collide with vertical baffle 32, shattering them into numerous even finer droplets. Simultaneously, during the rotation of the rotating disk 31, the side of baffle 32 can cut the droplets, creating a shearing effect. This increases the contact area between the two phases, enhancing the mass transfer effect and further improving the gas-liquid mass transfer rate of the high-gravity rotating bed.

[0055] In addition, such as Figure 1 and Figure 6 As shown, a gas-liquid distribution plate 4 can also be installed below the baffle unit 3. This gas-liquid distribution plate 4 is fixedly installed on the wall of the spherical reactor and does not rotate with the rotating shaft. Specifically, the gas-liquid distribution plate 4 is sleeved on the rotating shaft 2 and has a clearance fit with the rotating shaft 2. A liquid overflow hole 42 is provided near the rotating shaft 2. Figure 6 Two ventilation holes 41 are evenly spaced on the gas-liquid distribution plate 4 (two are provided in the middle). The gas-liquid distribution plate added in this invention can reduce the mist entrainment phenomenon that occurs in existing rotating beds, extend the service life of the device, and achieve long-term operation.

[0056] like Figure 7 As shown, the present invention also provides a second embodiment for the baffle unit 3. Figure 7 The baffle unit is located in the second spherical reactor 200, including rotating disks 31A and stationary disks 33A spaced apart along the axial direction of the rotation axis, that is, rotating disks and stationary disks are alternately arranged from top to bottom along the axial direction of the rotation axis. The rotating disk 31A is fixedly connected to the rotation shaft 2, and the stationary disk 33A is fixedly connected to the wall of the spherical reactor; the liquid flowing from top to bottom and the flue gas flowing from bottom to top form countercurrent and baffle at the baffle unit in the second embodiment, thereby realizing secondary gas-liquid mass transfer. Figure 7 The flow deflector unit in the second embodiment differs from the flow deflector in the first embodiment. The rotation of the rotating disk 31A can increase the gas-liquid disturbance in the flow deflector channel and form vortices locally, which is more conducive to gas-liquid mass transfer.

[0057] like Figure 8 As shown, this invention provides a process application of the aforementioned spherical reactor after denitrification and desulfurization, using the first spherical reactor 100 as an example. Inside the flue gas inlet pipeline 5, this invention provides an induced draft vane 51, which can be axial flow type, and its shape can be airfoil, fan-shaped, or plate-shaped. Correspondingly, an energy converter 6 is provided outside the flue gas inlet pipeline 5. This energy converter 6 can be an existing magnetic power generation device. The incoming flue gas passes through the induced draft vane 51, driving the vane to rotate continuously, generating current by cutting the magnetic field, and the electrical energy can be supplied to… Figure 8 The invention includes a liquid inlet pump 7 (i.e., a rich liquid pump) and a liquid outlet pump 8 (i.e., a lean liquid pump). By effectively utilizing the high flue gas velocity at the inlet, and ensuring the normal operation of the ultragravity rotating bed, the excess kinetic energy in the flue gas can be converted into electrical energy to provide power for the lean liquid pump, rich liquid pump, and other devices, thereby reducing [the following text is incomplete and requires further context: "reducing the [unclear text] " Figure 8 This reduces the overall energy loss of the system. Simultaneously, the flue gas velocity is actively reduced, effectively extending the residence time of the gas within the baffle unit. Experiments have shown that this improves the gas-liquid mass transfer efficiency of subsequent baffle units.

[0058] Further as Figure 8 As shown, the wet desulfurization tower 9 is located at the front end of the first spherical reactor 100, the regeneration tower 12 is located at the rear end of the first spherical reactor 100, the outlet of the liquid inlet pump 7 is connected to the liquid inlet of the spherical reactor, the lean and rich liquid heat exchanger 11 is connected to the liquid inlet pump 7 and the regeneration tower 12 respectively, the flue gas heat exchanger 13 is connected to the regeneration tower 12, the lean and rich liquid heat exchanger 11 is also connected to the outlet of the liquid outlet pump 8, and the inlet of the liquid outlet pump 8 is connected to the liquid outlet of the first spherical reactor 100. Furthermore, the first inlet of the lean-rich liquid heat exchanger 11 is connected to the outlet of the liquid outlet pump 8, and the first outlet of the lean-rich liquid heat exchanger 11 is connected to the upper part of the regeneration tower 12; the second inlet of the lean-rich liquid heat exchanger 11 is connected to the bottom of the regeneration tower 12, and the second outlet of the lean-rich liquid heat exchanger 11 is connected to the inlet of the liquid inlet pump 7; the flue gas outlet of the desulfurization tower 9 is connected to the flue gas inlet pipeline 5 of the first spherical reactor 100; the outlet of the first spherical reactor 100 is connected to the external space, and the flue gas is directly discharged to the atmosphere 15; the first inlet of the flue gas heat exchanger 13 is connected to the denitrification outlet flue gas 14, and the first outlet of the flue gas heat exchanger 13 is connected to the flue gas inlet of the wet desulfurization tower 9; the second inlet of the flue gas heat exchanger 13 is connected to the low-temperature steam of the regeneration tower 12, and the second outlet of the flue gas heat exchanger 13 is connected to the high-temperature steam of the regeneration tower 12.

[0059] Figure 8 The process shown is as follows: the denitrification outlet flue gas 14 enters the flue gas heat exchanger 13 and exchanges heat with the low temperature steam, and then enters the wet desulfurization tower 9. After desulfurization, the flue gas passes through the flue gas inlet pipeline 5, passes through the induced draft blades 51, and enters the first spherical reactor 100 of the present invention. The flue gas passes through the gas-liquid distribution plate, the baffle unit and the carbon capture unit, and finally leaves the reactor through the gas outlet pipe at the top of the reactor. The liquid (which can be alkaline) used as the carbon capture absorbent enters through the inlet at the top of the reactor, is sprayed out through nozzles to form an umbrella-shaped distribution, and then undergoes two gas-liquid mass transfer processes through the tree-shaped carbon capture unit and the baffle unit to capture carbon dioxide from the flue gas. Finally, it accumulates at the bottom of the reactor and is led out through the liquid outlet pipe to the liquid outlet pump 8. After passing through the lean-rich liquid heat exchanger 11, it enters the upper part of the regeneration tower 12 for absorbent regeneration. High-concentration carbon dioxide 16 leaves from the top of the tower as a product, while the regenerated lean liquid absorbent leaves from the bottom of the regeneration tower and enters the lean-rich liquid heat exchanger 11. After entering the liquid inlet pump 7, it returns to the first spherical reactor 100 through the liquid feed pipe. The induced draft vanes 51 installed in the flue gas inlet pipeline 5 convert mechanical energy into electrical energy, which is then delivered to the liquid inlet pump 7 and the liquid outlet pump 8 to reduce energy loss.

[0060] Example 1

[0061] A wet desulfurization system employs the apparatus and process of this invention. The flue gas flow rate at the desulfurization outlet is 100,000 cubic meters per hour, the carbon dioxide concentration in the flue gas is 15%, the flow velocity is 12 m / s, and the temperature is 60°C. MDEA solution is used as the absorbent. The tree-like carbon capture unit consists of 9 layers, with 4 baffles in each layer arranged in a cross shape. The rotating disk of the baffle unit rotates at approximately 800 r / min. The baffles on the rotating disk are arranged as follows: 6 baffles are installed at 60-degree intervals, with each ring of baffles spaced 100 mm apart from the previous ring.

[0062] The denitrification outlet flue gas (180℃) enters the flue gas heat exchanger and exchanges heat with low-temperature steam (40℃) before entering the wet desulfurization tower. After desulfurization, the flue gas enters the spherical reactor through the flue gas inlet pipeline and induced draft vanes. The flue gas and carbon dioxide absorbent liquid (MDEA) undergo two gas-liquid mass transfer processes in the dendritic carbon capture unit and the baffle unit. The liquid after carbon capture is led out through the liquid outlet pipe, passes through the lean-rich liquid heat exchanger, and enters the upper part of the regeneration tower for MDEA regeneration. The regenerated MDEA leaves from the bottom of the regeneration tower and enters the lean-rich liquid heat exchanger, and is then pumped back to the spherical reactor. The induced draft vanes and capacity converter convert the kinetic energy of the flue gas into electrical energy to power the liquid inlet pump and the liquid outlet pump.

[0063] Calculations show that the carbon dioxide capture rate is 80%, and the purity of the separated carbon dioxide is 90%. The converted electrical energy can provide an output of more than 400 kWh, and the overall process energy consumption is about 300 kWh.

[0064] Comparative Example

[0065] A certain wet desulfurization unit uses an existing high-gravity rotating bed, but does not convert the kinetic energy of the flue gas into power for the system. The flue gas flow rate at the desulfurization outlet is 100,000 cubic meters per hour, the carbon dioxide concentration in the flue gas is 15%, the flow velocity is 12 m / s, the temperature is 60℃, and MDEA solution is used as the absorbent. The rotational speed of the high-gravity rotating bed is approximately 800 r / min.

[0066] The denitrification outlet flue gas (180℃) directly enters the wet desulfurization tower. After desulfurization (60℃), the flue gas enters the high-gravity rotating bed and finally leaves the bed through the flue gas outlet pipe. MDEA enters through the liquid feed pipe and exits through the liquid discharge pipe. It passes through the lean-rich liquid heat exchanger and enters the upper part of the regeneration tower for MDEA regeneration. The regenerated MDEA leaves from the bottom of the regeneration tower and enters the lean-rich liquid heat exchanger. It is then pumped and returned to the shell through the liquid feed pipe.

[0067] Calculations show that the carbon dioxide capture rate is 60%, and the purity of the separated carbon dioxide is 75%. The overall energy consumption of the wet desulfurization process is approximately 1000 kW·h.

[0068] The foregoing description of specific exemplary embodiments of the present invention is for illustrative and explanatory purposes. These descriptions are not intended to limit the invention to the precise forms disclosed, and it will be apparent that many changes and variations can be made in accordance with the foregoing teachings. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application, thereby enabling those skilled in the art to implement and utilize various different exemplary embodiments of the invention, as well as various different choices and variations. Any simple modifications, equivalent changes, and alterations made to the foregoing exemplary embodiments should fall within the scope of protection of the present invention.

Claims

1. A carbon capture unit, characterized in that, Set within a spherical reactor, comprising: A rotating shaft is vertically inserted into the spherical reactor; The tree-shaped baffle is tree-shaped in general and is arranged in layers along the circumference of the axis of rotation. Each layer has multiple baffles that are evenly spaced apart, and the baffles in adjacent layers are offset from each other in the radial direction. The baffles are fixedly connected to the axis of rotation by connecting rods, and the connecting rod length of the lower layer baffle is greater than that of the upper layer baffle. During the rotation of the shaft, the liquid used for carbon capture impacts the baffle from top to bottom. The baffle breaks the liquid into fine droplets and causes the droplets to descend in a spiral motion. As they descend, they undergo gas-liquid mass transfer with the flue gas rising from bottom to top.

2. The carbon capture unit according to claim 1, characterized in that, Each of the baffles has an inclination angle that allows it to impact the liquid perpendicularly; the liquid originates from a liquid distributor located at the top of the spherical reactor.

3. The carbon capture unit according to claim 2, characterized in that, The tilt angle of the baffle decreases layer by layer from top to bottom.

4. The carbon capture unit according to claim 3, characterized in that, The uppermost baffle is positioned to match the height of the liquid distributor; the lowermost baffle is positioned close to the inner wall of the spherical reactor.

5. The carbon capture unit according to claim 1, characterized in that, The connecting rod has a flat cross-section, with one end fixedly connected to the baffle and the other end fixedly connected to the rotating shaft.

6. The carbon capture unit according to claim 1, characterized in that, The baffles are arranged in 5 to 10 layers, with each layer having an offset angle of 5° to 15°; each layer has 4 baffles.

7. A high-gravity rotating bed, characterized in that, Includes the carbon capture unit as described in any one of claims 1 to 6.

8. The high-gravity rotating bed according to claim 7, characterized in that, Also includes: A baffle unit, located below the carbon capture unit and at least part of which rotates with the shaft, is used to receive liquid from the carbon capture unit after gas-liquid mass transfer and flue gas from the bottom of the spherical reactor. Secondary gas-liquid mass transfer is performed through the countercurrent of liquid and flue gas and the baffle effect.

9. The high-gravity rotating bed according to claim 8, characterized in that, The baffle unit includes: A rotating disk is fixedly connected to the rotating shaft, and multiple concentric baffles extend downward from the disk surface, with multiple baffles in each concentric circle and evenly spaced apart. A stationary disk is fixedly connected to the wall of a spherical reactor. Multiple baffle rings extend upward from the disk surface, and the baffle rings are staggered from the baffles of the corresponding rings. The liquid entering from the outer edge of the rotating disk and the flue gas entering from the inner edge of the stationary disk form a countercurrent and a deflection, thereby realizing the secondary gas-liquid mass transfer.

10. The high-gravity rotating bed according to claim 9, characterized in that, The number of baffles is the same for each revolution of the rotating disk.

11. The high-gravity rotating bed according to claim 10, characterized in that, Each ring of the rotating disk has concentric baffles, with a total of 5 to 15 baffles and a baffle spacing that is an integer multiple of 50 mm. The baffles on the stationary disk are spaced at an integer multiple of 50 mm, and the distance between the baffles and the baffles is an integer multiple of 25 mm. Multiple rectangular liquid outlet holes are evenly distributed on the baffles.

12. The high-gravity rotating bed according to claim 8, characterized in that, The baffle unit includes a rotating disk and a stationary disk spaced apart along the axial direction of the rotating shaft. The rotating disk is fixedly connected to the rotating shaft, and the stationary disk is fixedly connected to the wall of the spherical reactor. The liquid flowing from top to bottom and the flue gas flowing from bottom to top form countercurrent and baffle in the baffle unit to realize the secondary gas-liquid mass transfer.

13. The high-gravity rotating bed according to claim 8, characterized in that, Below the baffle unit is a gas-liquid distribution plate, which is fixedly installed on the wall of the spherical reactor. The gas-liquid distribution plate is sleeved on the rotating shaft and is fitted with the rotating shaft with a clearance. A liquid overflow hole is provided near the rotating shaft. Ventilation holes are evenly spaced on the gas-liquid distribution plate.

14. The high-gravity rotating bed according to claim 13, characterized in that, The flue gas inlet of the spherical reactor is located at the bottom; The flue gas inlet is connected to an inlet pipeline, which is equipped with induced draft vanes. The rotational mechanical energy of the induced draft vanes is converted into electrical energy to power the liquid inlet pump and the liquid outlet pump.

Images