Desulfurization and decarburization rotating bed device and method

Abstract

The present invention discloses a desulfurization and decarburization rotating bed apparatus and method, the apparatus is a spherical reactor structure, and the apparatus comprises: a decarburization unit, which comprises a rotating shaft and a tree-shaped baffle plate, and the rotating shaft is vertically arranged in a spherical reactor in a penetrating manner; the whole tree-shaped baffles are tree-shaped and are arranged in a layered mode in the circumferential direction of the rotating shaft, the number of the baffles in each layer is multiple, the baffles are evenly arranged at intervals, and deviation angles are formed in the baffles of the adjacent layers in the radial direction. The connecting rod of the lower-layer baffle is longer than that of the upper-layer baffle; in the rotating process of the rotating shaft, the CO2 absorbent impacts the baffle plate from top to bottom, the baffle plate crushes liquid into fine fog drops and makes the fog drops descend spirally, and gas-liquid mass transfer is performed between the fog drops and flue gas from bottom to top while the fog drops descend; and the desulfurization unit is positioned below the decarburization unit and is used for forming contact mixing of the spirally ascending flue gas and the spirally descending SO2 absorbent. Desulfurization and decarburization processes are integrated in the same spherical reactor, so that the integration of desulfurization and decarburization is realized.

Description

Technical Field

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

[0002] Carbon dioxide emissions have become the focus of environmental protection, and the most widely used decarbonization technology is chemical absorption. At present, the absorption method is mostly carried out in traditional tower equipment (such as packed towers, plate towers, etc.), and gas-liquid contact is achieved under the action of the gravity field for mass transfer. Due to the weak gravity field, the liquid film flows slowly, the effective contact area per unit volume is small, and the volume mass transfer coefficient of the mass transfer process controlled by the liquid film is low, resulting in such equipment being bulky, with low space utilization and equipment production intensity.

[0003] Since petrochemical system equipment occupies a large area, adding a decarbonization system using amine liquid absorption method after the desulfurization system requires the installation of an absorption tower and a desorption tower after the desulfurization tower. In addition, new equipment such as heat exchangers, pumps, and storage tanks are also required. For mature flue gas purification systems, the placement of decarbonization process equipment is difficult to coordinate.

[0004] There are also integrated desulfurization and decarbonization equipment in the prior art. For example, Chinese patent application CN115738634A discloses an integrated pneumatic ammonia desulfurization and decarbonization system, which includes a desulfurization and decarbonization tower, a decomposition tower, an MGGH heat exchange system, a dilute ammonia storage tank, an oxidation tank, a primary water washing tank and a secondary water washing tank. This system uses ammonia water to achieve both efficient desulfurization and efficient decarbonization in the same device, so that SO2 and CO2 can be efficiently removed at the same time, and there is no adverse effect between the systems. In addition, a large amount of ammonia will escape during the absorption of CO2 by dilute ammonia water. The escaped ammonia enters the water washing section of the desulfurization system with the flue gas and is absorbed by water. The water containing a small amount of ammonia enters the desulfurization absorption system as make-up water, which can reduce the ammonia consumption of the absorption system. Although this method can remove sulfur and carbon at the same time, its removal efficiency is low, and ammonia has limited SO2 absorption capacity, which can easily cause SO2 emissions to exceed the standard and affect the normal production of the enterprise. At the same time, since this scheme still uses traditional tower equipment, and traditional tower equipment has limited gas-liquid mass transfer effect and large size, the height of the desulfurization and decarbonization tower is too high, which is prone to safety and environmental problems.

[0005] Therefore, there is an urgent need for a rotating bed device and method for desulfurization and decarbonization, which can not only avoid the problem of large volume of traditional tower equipment, but also effectively ensure the absorption rate of SO2 and CO2 and effectively improve the mass transfer effect.

[0006] The information disclosed in this background technology section is only intended to enhance the understanding of the overall background of the invention and should not be regarded as an acknowledgment 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 object of the present invention is to provide a desulfurization and decarbonization rotating bed device and method, which integrates the desulfurization and decarbonization processes in the same spherical reactor to achieve the integration of desulfurization and decarbonization.

[0008] Another object of the present invention is to provide a rotating bed device and method for desulfurization and decarbonization. Through the decarbonization unit that is tree-shaped and rotatable as a whole, the CO2 absorption rate can be effectively guaranteed and the mass transfer effect can be improved; the desulfurization unit can form gas-liquid contact between the spirally rising flue gas and the spirally descending SO2 absorbent, which can effectively extend the contact time between the gas and the liquid.

[0009] To achieve the above-mentioned purpose, according to the first aspect of the present invention, there is provided a desulfurization and decarbonization rotating bed device, which is a spherical reactor structure, comprising: a decarbonization unit, which comprises a rotating shaft and a tree-like baffle, and the rotating shaft is vertically arranged in the spherical reactor; the tree-like baffles are tree-shaped as a whole and are arranged in layers along the circumference of the rotating shaft, and the number of baffles in each layer is multiple and evenly spaced, and the baffles of adjacent layers are provided with a deviation angle in the radial direction; the baffles are fixedly connected to the rotating shaft by connecting rods, and the connecting rod length of the lower baffle is greater than that of the upper baffle; during the rotation of the rotating shaft, the CO2 absorbent hits the baffle from top to bottom, and the baffle breaks the liquid into fine droplets and causes the droplets to spirally descend, while descending, gas-liquid mass transfer is carried out with the flue gas from bottom to top; a desulfurization unit, which is located below the decarbonization unit, is used to form a contact and mixing between the spirally rising flue gas and the spirally descending SO2 absorbent.

[0010] Furthermore, in the above technical solution, each layer of baffles has an inclination angle, and the inclination angle satisfies the vertical collision with the CO2 absorbent; the CO2 absorbent comes from the liquid distributor arranged at the top of the spherical reactor. The inclination angle of the baffles can decrease layer by layer from top to bottom.

[0011] Furthermore, in the above technical solution, the baffle plate setting position can be adapted to the height of the liquid distributor; the baffle plate of the lowest layer can be set close to the inner wall of the spherical reactor.

[0012] Furthermore, in the above technical solution, the cross section of the connecting rod may be flat, with one end fixedly connected to the baffle and the other end fixedly connected to the rotating shaft.

[0013] Furthermore, in the above technical solution, the baffles can be arranged in 5 to 10 layers, and the deviation angle of each layer can be 5° to 15°; the number of baffles in each layer can be 4.

[0014] Furthermore, in the above technical solution, holes may be opened on the baffle, and the shape of the holes may be circular, square or triangular; the number of holes may be 1 to 4 and evenly distributed on the baffle.

[0015] Furthermore, in the above technical solution, the desulfurization unit may include: a nozzle, which is arranged below the decarbonization unit and connected to the absorbent pipeline, and the nozzle is fixed; a dynamic mixing cylinder, which is arranged below the nozzle and corresponds to the position of the nozzle, and the dynamic mixing cylinder is a cylindrical structure with openings at both ends, and the lower end is fixedly connected to a rotating disk, and the rotating disk can rotate with the rotating shaft; the rising flue gas in the mixing cylinder spirals up under the action of rotation, and the SO2 absorbent from the nozzle can spiral down after entering the mixing cylinder.

[0016] Furthermore, in the above technical solution, the absorbent pipes can extend in the horizontal direction and there can be multiple absorbent pipes, and the absorbent pipes and nozzles can be evenly distributed and the number can be determined according to the SO2 content in the flue gas.

[0017] Furthermore, in the above technical solution, an overflow hole may be provided on the rotating disk to prevent the absorbent from flooding the mixing cylinder and causing flooding.

[0018] Furthermore, in the above technical solution, a gas-liquid distribution plate may be provided under the desulfurization unit, and the gas-liquid distribution plate may be fixedly installed on the wall of the spherical reactor; the gas-liquid distribution plate may be sleeved on the rotating shaft and cooperate with the rotating shaft gap, a liquid overflow hole may be provided near the rotating shaft, and ventilation holes may be evenly spaced on the gas-liquid distribution plate.

[0019] To achieve the above-mentioned purpose, according to the second aspect of the present invention, a desulfurization and decarbonization method is provided, and the desulfurization and decarbonization processes are completed in the same spherical reactor, comprising the following steps: A. The flue gas after denitrification enters through the bottom of the reactor and is evenly distributed in the reactor with an upward trend; B. The rising flue gas enters the dynamic mixing cylinder and spirally rises in the cylinder under the action of rotation, and contacts and mixes with the SO2 absorbent from the nozzle and enters the cylinder in a spiral downward state in reverse, thereby executing the flue gas desulfurization process; C. The desulfurized flue gas continues to rise and enters the decarbonization process: through the overall rotation of the tree-like baffle, the CO2 absorbent hits the baffle from top to bottom, and the baffle breaks the liquid into fine droplets and causes the droplets to spiral downward, while descending, performing gas-liquid mass transfer with the desulfurized flue gas running from bottom to top; D. The purified flue gas is discharged into the atmosphere through the gas outlet at the top of the spherical reactor.

[0020] Furthermore, in the above technical scheme, the SO2 absorbent can be one or more of CaO, Ca(OH)2, CaCO3, Na2CO3, NaOH, KOH, NH3, NH4OH and NH4HCO3; the mass concentration of the alkaline solution can be 5 to 40%.

[0021] Furthermore, in the above technical solution, the CO2 absorbent may be one or more of Na2CO3, Na2SO3 and NaHCO3; and the mass concentration of the alkaline solution may be 5 to 40%.

[0022] Furthermore, in the above technical scheme, the SO2 absorbent and the CO2 absorbent can also use the same double desorption absorbent, which can be one or more of NaHCO3, NH3·H2O and NaOH; on this basis, the desulfurization process of the present invention can simultaneously decarbonize, and the decarbonization process can simultaneously desulfurize.

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

[0024] 1) The present invention adopts a rotatable baffle and a through hole is provided on the baffle. During the rotation process, the liquid absorbent is broken into finer droplets, which can effectively increase the overall mass transfer rate; at the same time, part of the liquid absorbent further changes its movement direction through the through hole on the baffle, and the droplets after the impact are further strengthened in the spiral downward trend, the travel of the droplets becomes longer, and while descending, the droplets carry out gas-liquid mass transfer with the flue gas from bottom to top, which can further increase the gas-liquid contact time and prolong the residence time of the flue gas in the decarbonization unit, thereby further improving the absorption effect of carbon dioxide;

[0025] 2) The baffles of adjacent layers in the decarbonization unit of the present invention, which is in a tree-like shape as a whole, are provided with a deviation angle in the radial direction, and the connecting rod length of the lower baffle is greater than the connecting rod length of the upper baffle, so that the baffle can receive the impact of liquid from different directions, reducing the possibility of direct drop of liquid, and in the state of overall rotation, it is more conducive to the spiral descent of droplets;

[0026] 3) In the decarbonization unit of the tree-like structure of the present invention, the length of the connecting rods of each layer is different, and increases layer by layer from top to bottom, so that the spiral descent of the droplets can be satisfied and the treatment amount of the flue gas can be ensured, and at the same time, the internal space of the spherical reactor can be fully utilized to minimize the liquid entering from the nozzle from falling directly into the lower space without collision;

[0027] 4) The flue gas is purified by combining the decarbonization unit and the desulfurization unit. After the gas and liquid complete the first gas-liquid mass transfer in the tree-shaped decarbonization unit, the decarbonization absorbent enters the desulfurization unit for secondary gas-liquid mass transfer. The desulfurization absorbent enters the reactor through the nozzle of the desulfurization unit. The desulfurization absorbent changes the flow direction of the absorbent through the nozzle and enters the dynamic mixing cylinder to contact the flue gas, thereby improving the mixing uniformity of the desulfurization absorbent and the flue gas; during the rotation of the rotating disk, the dynamic mixing cylinder can change the flow direction of the flue gas and the desulfurization absorbent, respectively showing a spiral upward and downward trend, thereby enhancing the mixing and mass transfer effect and further improving the gas-liquid mass transfer rate of the desulfurization unit;

[0028] 5) By combining the decarbonization unit and the desulfurization unit of the present invention, the rotation of the rotating disk of the desulfurization unit can increase the gas-liquid disturbance in the mixing barrel channel and form a vortex locally, which is more conducive to gas-liquid mass transfer;

[0029] 6) The arrangement of the gas-liquid distribution plate below the desulfurization unit of the present invention can reduce the phenomenon of mist entrainment and liquid flooding in the existing rotating bed, extend the operating life of the device, and achieve long-term operation;

[0030] 7) The present invention adopts a new type of high-efficiency integrated desulfurization and decarbonization process. The decarbonization absorbent and the desulfurization absorbent can synergistically remove CO2 and SO2. The two absorbents complement each other (or use a double desorbent) to avoid problems such as equipment scaling and clogging due to excessive absorbent input; a rotating bed is used as a reactor (the high-speed rotation of the rotating bed can generate a gravity field of 10 to 1000g), and the reactor is set to a spherical shape. While ensuring the absorption rate of SO2 and CO2, the space of the spherical reactor can be fully utilized, the equipment volume can be reduced, and safety and environmental protection problems can be avoided; this ultra-gravity reactor is flexible in operation, the equipment is easy to move, and the performance is far superior to traditional tower equipment.

[0031] 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 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 the accompanying drawings as follows. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 It is a schematic diagram of the internal structure of the desulfurization and decarbonization rotating bed device of the present invention (showing the structures of the desulfurization unit and the decarbonization unit; the solid arrows in the figure indicate the flow direction of the liquid absorbent, and the dotted arrows indicate the flow direction of the flue gas).

[0033] Figure 2 It is a top view schematic diagram of the decarburization unit of the present invention.

[0034] Figure 3 It is a schematic diagram of the baffle structure in the decarbonization unit of the present invention.

[0035] Figure 4 It is a schematic diagram of the arrangement of absorbent pipelines and nozzles in the desulfurization unit of the present invention.

[0036] Figure 5 It is a schematic top view of the rotating disk in the desulfurization unit of the present invention.

[0037] Figure 6 It is a top view schematic diagram of the gas-liquid distribution plate of the present invention.

[0038] Figure 7 It is a schematic diagram of the application of the desulfurization and decarbonization rotating bed device of the present invention.

[0039] Description of main reference numerals:

[0040] 100-spherical reactor, 101-decarbonization absorbent liquid inlet, 102-gas outlet, 103-gas inlet, 104-desulfurization absorbent liquid inlet, 105-liquid outlet; 200-denitrification device, 201-denitrification outlet flue gas pipeline, 300-regeneration tower, 400-flue gas heat exchanger, 500-lean and rich liquid heat exchanger, 501-decarbonization absorbent inlet pump, 502-desulfurization absorbent inlet pump, 503-absorbent outlet pump;

[0041] 1-desulfurization unit, 11-nozzle, 12-absorbent pipeline, 13-dynamic mixing cylinder, 14-overflow hole; 2-decarbonization unit, 21-baffle, 22-through hole, 23-connecting rod; 3-rotating shaft, 4-rotating disk, 5-gas-liquid distribution plate, 51-vent, 52-liquid overflow hole. DETAILED DESCRIPTION

[0042] The specific implementation modes of the present invention are described in detail below in conjunction with the accompanying drawings, but it should be understood that the protection scope of the present invention is not limited by the specific implementation modes.

[0043] Unless explicitly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising”, etc., will be understood to include the stated elements or components but not to exclude other elements or components.

[0044] In this document, for the convenience of description, spatial relative terms such as "below", "below", "down", "above", "above", "upper", etc. may be used to describe the relationship between one element or feature and another element or feature in the accompanying drawings. It should be understood that the spatial relative terms are intended to include different orientations of the object in use or operation in addition to the orientation depicted in the figure. 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. Objects may also have other orientations (rotated 90 degrees or other orientations) and the spatial relative terms used in this document should be interpreted accordingly.

[0045] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit a specific position or relative relationship. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable.

[0046] like Figure 1As shown, the present invention provides a desulfurization and decarbonization rotating bed device, which is a spherical reactor 100 structure, including a decarbonization unit 2 and a desulfurization unit 1, and can be used to complete desulfurization and decarbonization of flue gas after denitration in the same reactor. The decarbonization unit 2 includes a rotating shaft 3 and a tree-like baffle, and the rotating shaft 3 is vertically penetrated in the spherical reactor 100, and a dynamic seal is provided at the penetration position. The tree-like baffle is tree-shaped as a whole and is arranged in layers along the circumference of the rotating shaft 3. The number of baffles 21 in each layer is multiple and evenly spaced, and the baffles 21 of adjacent layers are provided with a deviation angle in the radial direction. The baffle 21 is fixedly connected to the rotating shaft 3 through a connecting rod 23, and the connecting rod length of the lower baffle is greater than the connecting rod length of the upper baffle; during the rotation of the rotating shaft 3, the CO2 absorbent hits the baffle 21 from top to bottom, and the baffle 21 breaks the liquid into fine droplets and causes the droplets to spirally descend, while descending, gas-liquid mass transfer is carried out with the flue gas from bottom to top. Preferably, but not restrictively, the baffle 21 may be provided with through holes 22 of different shapes, and the shape of the holes may be circular, square or triangular, etc.; the number of holes is 1 to 4 and is evenly distributed on the baffle. The design of the through holes can better change the flow direction of the liquid, and the spiral descent effect of the droplets is better, which is more conducive to the gas-liquid mass transfer process. The desulfurization unit 1 is located below the decarbonization unit 2, and is used to form a contact and mixing of the spirally ascending flue gas and the spirally descending SO2 absorbent.

[0047] The decarbonization unit of the present invention, which is composed of a rotatable baffle, baffle through holes and connecting rods, is formed in a tree-like shape, so that the baffle 21 is substantially perpendicular to the falling direction of the liquid (i.e., the CO2 absorbent). During the rotation process, the liquid can be broken into smaller droplets, which can effectively increase the overall mass transfer rate. At the same time, the through holes 22 can further change the flow direction of the liquid, and the droplets after impact fall in a spiral manner, and the travel distance of the droplets becomes longer, which can effectively increase the gas-liquid contact time, thereby further improving the absorption effect of carbon dioxide. The baffles 21 of adjacent layers are provided with a deviation angle in the radial direction (reference Figure 2 The top view of the device is shown in FIG. 2 ), and the connecting rod length of the lower baffle is greater than that of the upper baffle, so that the baffle 21 can be impacted by liquid from different directions, reducing the possibility of direct liquid falling. In the state of overall rotation, it is more conducive to the spiral descent of the droplets. The desulfurization unit 1 is arranged in the same spherical reactor 100 as the decarbonization unit 2, so that the flue gas after denitrification can be desulfurized and decarbonized in an integrated manner, which not only reduces the space occupied by the equipment, but also saves investment. The desulfurization unit realizes sufficient mixing and mass transfer of gas and liquid in a limited space through the spiral operation of the ascending flue gas and the descending SO2 absorbent.

[0048] Further Figures 1 to 3 As shown, each baffle 21 has an inclination angle (i.e., inwardly inclined, refer to Figure 3), the setting of the inclination angle is preferably to meet the vertical collision with the CO2 absorbent. The CO2 absorbent comes from the liquid distributor arranged at the top of the spherical reactor, that is, the distributor arranged at the bottom of the liquid inlet 101. The liquid sprayed from the nozzle of the distributor is distributed in an umbrella shape so as to better collide with the baffle 21 of each layer. Due to the difference in the spray coverage angle and the spray stroke of the nozzle, the inclination angle of the baffle can be set to decrease layer by layer from top to bottom. Furthermore, the setting position of the baffle of the topmost layer is adapted to the height of the liquid distributor, and the setting position of the baffle of the bottommost layer is close to the inner wall of the spherical reactor. Since the present invention adopts a spherical reactor and a decarbonization unit with an overall tree-like structure, the length of each layer of connecting rods 23 is not the same, and increases layer by layer from top to bottom. This can not only meet the spiral descent of the droplets and ensure the treatment capacity of the flue gas, but also make full use of the internal space of the spherical reactor 100 to minimize the liquid entering from the nozzle from falling directly to the lower space without collision. Further, preferably but not restrictively, the cross section of the connecting rod 23 can be designed to be flat, so that the connecting rod itself can also be hit by the liquid, thereby better achieving the atomization effect. One end of the connecting rod 23 is fixedly connected to the baffle 21, and the other end is fixedly connected to the rotating shaft 3, so that each layer of the baffle 21 can rotate with the rotating shaft 3. Specifically, according to the inner diameter of the spherical reactor, the baffles are preferably arranged in 5 to 10 layers, and the deviation angle of each layer is 5° to 15°. The baffles of each layer can be set to 4 and arranged in a cross shape (refer to Figure 2 ).

[0049] Further Figure 1 , 4 As shown in Figures 5 and 6, the desulfurization unit 1 of the present invention at least includes a nozzle 11 and a dynamic mixing drum 13. The nozzle 11 is arranged below the decarbonization unit 2 and is connected to the absorbent pipe 12. The nozzle is fixed and is arranged as a static nozzle. The dynamic mixing drum 13 is arranged below the nozzle 11 and corresponds to the position of the nozzle. The dynamic mixing drum 13 is a cylindrical structure with openings at both ends, and the lower end is fixedly connected to the rotating disk 4, and the rotating disk 4 can rotate with the rotating shaft 3. The rising flue gas in the dynamic mixing drum 13 spirally rises under the action of the rotation of the rotating disk, and the SO2 absorbent from the nozzle spirally descends after entering the mixing drum. Specifically, refer to Figure 4, the uniformly arranged nozzles 11 are arranged on the absorbent pipeline 12, and the absorbent pipeline 12 is arranged in the spherical reactor 100. The SO2 absorbent changes the flow direction of the absorbent through the nozzle 11, enters the dynamic mixing cylinder 13 and contacts with the flue gas. Since the dynamic mixing cylinder 13 is arranged below the nozzle 11 and is fixedly connected to the rotating disk 4, when the rotating disk 4 rotates at high speed with the rotating shaft 3, the flue gas in the mixing cylinder shows a spiral upward trend, and the SO2 absorbent in the mixing cylinder shows a spiral downward trend. The contact time of gas and liquid is longer, and the mixing and mass transfer is more sufficient. 2-6 overflow holes 14 are opened on the rotating disk 4 to prevent the liquid from flooding the dynamic mixing cylinder 13 and causing liquid flooding. The desulfurization unit composed of the nozzle 11, the dynamic mixing cylinder 13 and the rotating disk 4 of the present invention changes the flow direction of the SO2 absorbent, thereby improving the mixing uniformity of the absorbent and the flue gas. The rotation of the dynamic mixing cylinder 13 makes the SO2 absorbent and the flue gas show a spiral downward and upward trend, accelerates the mixing, enhances the mixing and mass transfer effect, and thus improves the utilization rate of the SO2 absorbent. The inventor has proved through experiments that the gas-liquid mass transfer efficiency between the SO2 absorbent and the flue gas is higher by adopting the arrangement mode of the dynamic mixing cylinder and the static nozzle of the present invention.

[0050] Further references Figure 4 , the absorbent pipeline 12 runs north-south (i.e. Figure 4 2-4 in the vertical direction, 2-4 in the east-west direction (i.e. Figure 4 In the horizontal direction), each absorbent pipeline is provided with 4-10 nozzles 11, and the number of pipelines and nozzles is determined according to the actual SO2 content in the flue gas. Figure 5 The dynamic mixing cylinders 13 are arranged in rows of 6 to 10 in the radial direction of the rotating disk 4, and can be arranged in 2 to 4 rows and evenly spaced according to needs.

[0051] Further Figure 1 and 6 As shown, a gas-liquid distribution plate 5 can also be arranged below the desulfurization unit 1. The gas-liquid distribution plate 5 is fixedly mounted on the wall of the spherical reactor 100 and does not rotate with the rotating shaft. Specifically, the gas-liquid distribution plate 5 is sleeved on the rotating shaft 3 and is in clearance with the rotating shaft 3. A liquid overflow hole 52 ( Figure 6 Two are arranged in the middle), and the gas-liquid distribution plate 5 is also evenly spaced with ventilation holes 51. The gas-liquid distribution plate added in the present invention can reduce the mist entrainment phenomenon in the existing rotating bed, extend the operating life of the device, and realize long-term operation.

[0052] Combination Figure 1 As shown, the present invention also provides a desulfurization and decarbonization process method, which is completed in the same spherical reactor and includes the following steps:

[0053] In step S101, the flue gas after denitration enters through the bottom of the spherical reactor 100 and is evenly distributed in the reactor with an upward trend.

[0054] In step S102, the rising flue gas enters the dynamic mixing cylinder 13 and spirally rises in the cylinder under the action of rotation, and contacts and mixes with the SO2 absorbent from the nozzle and spirally descends in the cylinder, and performs the flue gas desulfurization process. The SO2 absorbent can be one or more of CaO, Ca(OH)2, CaCO3, Na2CO3, NaOH, KOH, NH3, NH4OH and NH4HCO3; the mass concentration of the alkaline solution is 5-40%.

[0055] Step S103, the flue gas after desulfurization continues to rise and enters the decarbonization process: through the overall rotation of the tree-shaped baffle, the CO2 absorbent hits the baffle 21 from top to bottom, and the baffle 21 breaks the liquid into fine droplets and makes the droplets spiral down, while descending, gas-liquid mass transfer is carried out with the flue gas after desulfurization running from bottom to top. The CO2 absorbent can be one or more of Na2CO3, Na2SO3 and NaHCO3; the mass concentration of the alkaline solution is 5-40%.

[0056] In step S104 , the purified flue gas is discharged into the atmosphere through the gas outlet 102 at the top of the spherical reactor 100 .

[0057] It should be noted that the SO2 absorbent involved in step S102 and the CO2 absorbent involved in step S103 can also use the same double desorption absorbent, which can be one or more of NaHCO3, NH3·H2O and NaOH. On this basis, the desulfurization process of the present invention can simultaneously decarbonize, and correspondingly, the decarbonization process can also simultaneously desulfurize.

[0058] Combine the following Figure 7 The industrial application process of the desulfurization and decarbonization rotating bed device of the present invention after flue gas denitrification is described in detail:

[0059] The flue gas denitrated by the denitrification device 200 enters the flue gas heat exchanger 400 through the denitrification outlet flue gas pipe 201 to exchange heat with the low-temperature steam, and then enters the spherical reactor 100. After the flue gas undergoes the aforementioned desulfurization and decarbonization process in the spherical reactor 100, it leaves the reactor through the gas outlet 102 at the top of the reactor. The liquid (alkaline solution can be used) serving as the desulfurization and decarbonization absorbent enters from the top and middle absorbent pipelines of the reactor (pumped by the decarbonization absorbent inlet pump 501 and the desulfurization absorbent inlet pump 502 respectively), is sprayed out through the nozzle to form an umbrella-shaped distribution, and then passes through the tree-like decarbonization unit 2 and the desulfurization unit 1 for gas-liquid mass transfer to remove sulfur dioxide and carbon dioxide in the flue gas (using double desorbents), and finally gathers at the bottom of the reactor and is led out from the liquid discharge pipe to the absorbent outlet pump 503, passes through the lean-rich liquid heat exchanger 500 and enters the upper part of the regeneration tower 300 for the absorbent regeneration process. The regenerated lean liquid absorbent leaves the bottom of the regeneration tower 300 and enters the lean-rich liquid heat exchanger 500, enters the decarbonization absorbent inlet pump 501 and the desulfurization absorbent inlet pump 502, and then returns to the first spherical reactor 100 through the liquid feed pipe.

[0060] Example 1

[0061] A catalytic cracking system adopts the device and process of the present invention, the flue gas flow rate of denitration outlet is 100,000 cubic meters per hour, and the sulfur dioxide concentration in the flue gas is 800 mg / Nm 3 , the carbon dioxide concentration is 15%, the flow rate is 12m / s, the temperature is 180℃, sodium bicarbonate solution is used as the decarbonation absorbent, and sodium hydroxide is used as the desulfurization absorbent. The tree-like decarbonization unit adopts 9 layers, and each layer has 4 baffles arranged in a cross shape. Each baffle has 4 through holes. The speed of the rotating disk of the desulfurization unit is about 800r / min. There are 2 absorbent pipelines running north-south and 2 running east-west. Each absorbent pipeline is equipped with 6 nozzles, and 6 dynamic mixing cylinders are arranged along the radial direction of the rotating disk, and are evenly arranged on 2 diameters.

[0062] The flue gas (180℃) at the outlet of denitrification enters the flue gas heat exchanger and exchanges heat with low-temperature steam (40℃), and then enters the spherical reactor. After desulfurization and decarbonization, the flue gas leaves the reactor through the top of the reactor. The sodium hydroxide solution enters from the top and middle absorbent pipelines of the reactor. The flue gas and sodium bicarbonate solution complete gas-liquid mass transfer in the decarbonization unit to remove carbon dioxide from the flue gas. The flue gas and sodium hydroxide solution complete gas-liquid mass transfer in the desulfurization unit to remove sulfur dioxide from the flue gas. After the two absorbents gather at the bottom of the reactor, they are led out from the liquid discharge pipe to the absorbent outlet pump and enter the waste liquid treatment device at the bottom of the tower.

[0063] According to calculations, the sulfur dioxide removal rate is 95%, the carbon dioxide removal rate is 80%, the absorbent utilization rate is 75%, and the overall equipment footprint is reduced by 50%.

[0064] Example 2

[0065] A catalytic cracking system adopts the device and process of the present invention, the flue gas flow rate of denitration outlet is 120,000 cubic meters per hour, and the sulfur dioxide concentration in the flue gas is 800 mg / Nm 3 , the carbon dioxide concentration is 15%, the flow rate is 12m / s, the temperature is 180℃, and the sodium bicarbonate solution is used as the absorbent. The tree-like decarbonization unit adopts 9 layers, and the baffles of each layer are set to 4 and arranged in a cross shape. Each baffle is provided with 4 through holes. The rotation speed of the rotating disk of the desulfurization unit is about 800r / min. There are 2 absorbent pipelines running north-south and 2 running east-west. Each absorbent pipeline is provided with 6 nozzles, and 6 dynamic mixing cylinders are set along the radial direction of the rotating disk, and are evenly arranged on 2 diameters.

[0066] The flue gas (180℃) at the outlet of denitrification enters the flue gas heat exchanger and exchanges heat with low-temperature steam (40℃), and then enters the spherical reactor. After desulfurization and decarbonization, the flue gas leaves the reactor through the top of the reactor. The sodium bicarbonate solution enters from the top and middle absorbent pipelines of the reactor. The flue gas and sodium bicarbonate solution complete two gas-liquid mass transfers in the decarbonization unit and the desulfurization unit to remove sulfur dioxide and carbon dioxide in the flue gas. Finally, after gathering at the bottom of the reactor, it is led out from the liquid discharge pipe to the absorbent outlet pump, passes through the lean-rich liquid heat exchanger and enters the upper part of the regeneration tower to carry out the absorbent regeneration process. The regenerated absorbent leaves the bottom of the regeneration tower and enters the lean-rich liquid heat exchanger, enters the decarbonization absorbent inlet pump and the desulfurization absorbent inlet pump, and then returns to the spherical reactor through the liquid feed pipe.

[0067] According to calculations, the sulfur dioxide removal rate is 98%, the carbon dioxide removal rate is 85%, the absorbent utilization rate is 85%, and the overall equipment footprint is reduced by 50%.

[0068] Comparative Example

[0069] A traditional carbon capture device is added to a traditional wet desulfurization device 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 800 mg / Nm 3 , carbon dioxide concentration is 15%, flow rate is 12m / s, temperature is 180℃, sodium bicarbonate solution is used as decarbonization absorbent, and sodium hydroxide is used as desulfurization absorbent.

[0070] The flue gas at the denitrification outlet (180℃) directly enters the wet desulfurization tower. After the flue gas is desulfurized (60℃), it enters the carbon capture device and finally leaves the device through the flue gas outlet pipe. The sodium bicarbonate solution enters from the liquid feed pipe, is led out from the liquid discharge pipe, passes through the lean-rich liquid heat exchanger and enters the upper part of the regeneration tower to carry out the absorbent regeneration process. The regenerated sodium bicarbonate leaves the bottom of the regeneration tower and enters the lean-rich liquid heat exchanger, and then is pumped back to the carbon capture device through the liquid feed pipe.

[0071] According to calculation, the carbon dioxide removal rate is 80%, the sulfur dioxide removal rate is 95%, the absorbent utilization rate is 65%, and the overall wet desulfurization and decarbonization process device covers an area of ​​4 times that of Example 1.

[0072] The foregoing description of specific exemplary embodiments of the present invention is for the purpose of illustration and demonstration. These descriptions are not intended to limit the present invention to the precise form disclosed, and it is clear that many changes and variations can be made based on the above teachings. The purpose of selecting and describing the exemplary embodiments is to explain the specific principles of the present invention and its practical application, so that those skilled in the art can realize and utilize various different exemplary embodiments of the present invention and various different selections and changes. Any simple modifications, equivalent changes and modifications made to the above exemplary embodiments should fall within the scope of protection of the present invention.

Claims

1. A desulfurization and decarbonization rotating bed device, characterized in that: It is a spherical reactor structure, comprising: A decarbonization unit, comprising a rotating shaft and a tree-like baffle, wherein the rotating shaft is vertically arranged in a spherical reactor; the tree-like baffle is in a tree shape as a whole and is arranged in layers along the circumference of the rotating shaft, wherein each layer has a plurality of baffles and is evenly spaced, and baffles of adjacent layers are provided with a deviation angle in the radial direction; the baffle is fixedly connected to the rotating shaft through a connecting rod, and the connecting rod length of the lower baffle is greater than that of the upper baffle; during the rotation of the rotating shaft, the CO2 absorbent hits the baffle from top to bottom, and the baffle breaks the liquid into fine droplets and causes the droplets to spirally descend, while performing gas-liquid mass transfer with the flue gas from bottom to top; The desulfurization unit is located below the decarbonization unit and is used to form a contact and mixing process between the spirally ascending flue gas and the spirally descending SO2 absorbent.

2. The desulfurization and decarbonization rotating bed device according to claim 1, characterized in that: Each layer of the baffles has an inclination angle, and the inclination angle is sufficient to collide vertically with the CO2 absorbent; the CO2 absorbent comes from a liquid distributor arranged on the top of the spherical reactor.

3. The desulfurization and decarbonization rotating bed device according to claim 2, characterized in that: The inclination angle of the baffle decreases layer by layer from top to bottom.

4. The desulfurization and decarbonization rotating bed device according to claim 3, characterized in that: The baffle plate of the uppermost layer is arranged at a position that matches the height of the liquid distributor; the baffle plate of the lowermost layer is arranged at a position that is close to the inner wall of the spherical reactor.

5. The desulfurization and decarbonization rotating bed device according to claim 1, characterized in that: The connecting rod has a flat cross section, one end of which is fixedly connected to the baffle, and the other end of which is fixedly connected to the rotating shaft.

6. The desulfurization and decarbonization rotating bed device according to claim 1, characterized in that: The baffles are arranged in 5 to 10 layers, and the deviation angle of each layer is 5° to 15°; the number of baffles in each layer is 4.

7. The desulfurization and decarbonization rotating bed device according to claim 1, characterized in that: The baffle plate is provided with holes, and the shape of the holes is circular, square or triangular; the number of the holes is 1 to 4 and they are evenly distributed on the baffle plate.

8. The desulfurization and decarbonization rotating bed device according to claim 1, characterized in that: The desulfurization unit comprises: A nozzle, which is arranged below the decarbonization unit and is connected to the absorbent pipeline, and the nozzle is fixed; A dynamic mixing cylinder is arranged below the nozzle and corresponds to the position of the nozzle. The dynamic mixing cylinder is a cylindrical structure with openings at both ends, and the lower end is fixedly connected to a rotating disk, and the rotating disk rotates with the rotating shaft; the rising flue gas in the mixing cylinder spirally rises under the action of rotation, and the SO2 absorbent from the nozzle enters the mixing cylinder and spirally descends.

9. The desulfurization and decarbonization rotating bed device according to claim 8, characterized in that: The absorbent pipelines extend in a horizontal direction and are in multiple numbers. The absorbent pipelines and nozzles are evenly distributed and the number is determined according to the SO2 content in the flue gas.

10. The desulfurization and decarbonization rotating bed device according to claim 8, characterized in that: The rotating disk is provided with an overflow hole to prevent the absorbent from flooding the mixing cylinder and causing flooding.

11. The desulfurization and decarbonization rotating bed device according to claim 8, characterized in that: A gas-liquid distribution plate is provided below the desulfurization unit and is fixedly mounted on the wall of the spherical reactor; the gas-liquid distribution plate is sleeved on the rotating shaft and fits in the rotating shaft gap, a liquid overflow hole is provided near the rotating shaft, and ventilation holes are evenly spaced on the gas-liquid distribution plate.

12. A desulfurization and decarbonization method, characterized in that: The desulfurization and decarbonization process is completed in the same spherical reactor and includes the following steps: A. The flue gas after denitrification enters through the bottom of the reactor and is evenly distributed in the reactor with an upward trend; B. The rising flue gas enters the dynamic mixing cylinder and rises in a spiral state in the cylinder under the action of rotation, and contacts and mixes with the SO2 absorbent that comes from the nozzle and enters the cylinder in a spiral downward state in reverse direction, thus executing the flue gas desulfurization process; C. The desulfurized flue gas continues to rise and enters the decarbonization process: through the overall rotation of the tree-shaped baffle, the CO2 absorbent hits the baffle from top to bottom, and the baffle breaks the liquid into fine droplets and makes the droplets spiral downward. While descending, the droplets conduct gas-liquid mass transfer with the desulfurized flue gas running from bottom to top; D. The purified flue gas is discharged into the atmosphere through the gas outlet at the top of the spherical reactor.

13. The desulfurization and decarbonization method according to claim 12, characterized in that: The SO2 absorbent is one or more of CaO, Ca(OH)2, CaCO3, Na2CO3, NaOH, KOH, NH3, NH4OH and NH4HCO3; the mass concentration of the alkaline solution is 5-40%.

14. The desulfurization and decarbonization method according to claim 12, characterized in that: The CO2 absorbent is one or more of Na2CO3, Na2SO3 and NaHCO3; the mass concentration of the alkaline solution is 5-40%.

15. The desulfurization and decarbonization method according to claim 12, characterized in that: The SO2 absorbent and the CO2 absorbent use the same double desorbent, which is one or more of NaHCO3, NH3·H2O and NaOH; on this basis, the desulfurization process simultaneously decarbonizes, and the decarbonization process simultaneously desulfurizes.

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