Desulfurization and decarburization rotating bed apparatus and method

Abstract

The application discloses a desulfurization and decarburization rotating bed device and method, which is a spherical reactor structure and comprises a decarburization unit and a desulfurization unit. The decarburization unit comprises a rotating shaft and a tree-shaped baffle, the rotating shaft is vertically arranged in the spherical reactor, the tree-shaped baffle is integrally arranged in a tree shape and is circumferentially layered, the number of baffles in each layer is multiple and the baffles are uniformly arranged at intervals, and the baffles in adjacent layers are arranged at a deviation angle in the radial direction. The baffle is fixedly connected with the rotating shaft through a connecting rod, 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, the CO2 absorbent impacts the baffle from top to bottom, the baffle breaks the liquid into small droplets and makes the droplets spiral downward, and the downward droplets perform gas-liquid mass transfer with flue gas rising from bottom to top. The desulfurization unit is arranged below the decarburization unit and is used for forming contact and mixing of the spiral upward flue gas and the spiral downward SO2 absorbent. The desulfurization and decarburization processes are integrated in the same spherical reactor, and the integration of desulfurization and decarburization is realized.

Description

TECHNICAL FIELD

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

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

[0003] Due to the large area occupied by petrochemical system devices, the addition of an amine liquid absorption method decarbonization system after the desulfurization system requires the installation of an absorption tower and a desorption tower after the desulfurization tower. In addition, new heat exchangers, pumps, storage tanks and other equipment need to be added. For mature flue gas purification systems, it is difficult to coordinate the placement of decarbonization process equipment.

[0004] There are also desulfurization and decarbonization integrated devices in the prior art. For example, Chinese patent application CN115738634A discloses a pneumatic ammonia desulfurization and decarbonization integrated system, which includes a desulfurization and decarbonization tower, a desorption tower, an MGGH heat exchange system, a dilute ammonia water storage tank, an oxidation tank, a primary water washing water tank and a secondary water washing water tank. This system uses ammonia water to achieve efficient desulfurization and decarbonization in the same device, so that SO2 and CO2 can be efficiently removed at the same time, and there is no mutual adverse effect between the systems. In addition, the absorption of CO2 by dilute ammonia water produces a large amount of ammonia escape, which 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 is used as make-up water to enter the desulfurization absorption system, which can reduce the ammonia consumption of the absorption system. Although this method can simultaneously desulfurize and decarbonize, the removal efficiency is low, the SO2 absorption capacity of ammonia water is limited, and SO2 emission may exceed the standard, affecting normal production of the enterprise. At the same time, since this scheme still uses traditional tower equipment, the gas-liquid mass transfer effect of the traditional tower equipment is limited, the desulfurization and decarbonization tower is too high, and safety and environmental problems are likely to occur.

[0005] Therefore, there is an urgent need for a desulfurization and decarbonization rotating bed device and method that 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 section is only intended to increase an understanding of the general context of the present application and should not be taken as an acknowledgement or any form of suggestion that this information constitutes prior art. SUMMARY

[0007] The present application aims to provide a desulfurization and decarburization rotating bed device and method, which integrates the desulfurization and decarburization processes in the same spherical reactor to realize the integration of desulfurization and decarburization.

[0008] Another object of the present application is to provide a desulfurization and decarburization rotating bed device and method, which can effectively ensure the CO2 absorption rate and improve the mass transfer effect through the decarburization unit which is overall tree-shaped and rotatable; and can effectively prolong the contact time between gas and liquid through the desulfurization unit which can form the gas-liquid contact of the spirally ascending flue gas and the spirally descending SO2 absorbent.

[0009] To achieve the above object, according to the first aspect of the present application, the present application provides a desulfurization and decarburization rotating bed device, which is a spherical reactor structure, comprising: a decarburization unit, which comprises a rotating shaft and a tree-shaped baffle, the rotating shaft being vertically arranged in the spherical reactor; the tree-shaped baffle is overall tree-shaped and is arranged in layers along the circumference of the rotating shaft, the number of baffles in each layer is multiple and is uniformly arranged, and the baffles of adjacent layers are arranged with a deviation angle in the radial direction; the baffle is fixedly connected with the rotating shaft through a connecting rod, and the length of the connecting rod of the lower baffle is greater than that of the connecting rod of the upper baffle; in the rotating process of the rotating shaft, the CO2 absorbent hits the baffle from top to bottom, the baffle breaks the liquid into fine droplets and makes the droplets spirally descend, and the descending droplets simultaneously perform gas-liquid mass transfer with the flue gas ascending from bottom to top; a desulfurization unit is arranged below the decarburization unit to form the contact and mixing of the spirally ascending flue gas and the spirally descending SO2 absorbent.

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

[0011] Further, in the above technical solution, the position of the baffle can be matched with the height of the liquid distributor; the position of the lowermost baffle can be close to the inner wall of the spherical reactor.

[0012] Further, in the above technical solution, the cross section of the connecting rod can be flat, one end of which is fixedly connected with the baffle, and the other end of which is fixedly connected with the rotating shaft.

[0013] Further, in the above technical solution, the baffle 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] Further, in the above technical solution, holes can be arranged on the baffle, and the shape of the holes can be circular, square or triangular; the number of holes can be 1 to 4 and uniformly distributed on the baffle.

[0015] Further, in the technical scheme, the desulfurization unit can comprise: a nozzle arranged below the decarburization unit and communicated with the absorbent pipeline, the nozzle being fixed; a dynamic mixing cylinder arranged below the nozzle and corresponding to the position of the nozzle, the dynamic mixing cylinder being a cylinder structure with both ends open, and the lower end being fixedly connected with a rotating disc, the rotating disc being rotatable with the rotating shaft; the flue gas rising in the mixing cylinder spirally rises under the action of rotation, and the SO2 absorbent from the nozzle spirally descends after entering the mixing cylinder.

[0016] Further, in the technical scheme, the absorbent pipeline can extend in the horizontal direction and the number of the absorbent pipelines can be multiple, and the absorbent pipelines and the nozzles can be uniformly distributed and the number of the absorbent pipelines and the nozzles can be determined according to the content of SO2 in the flue gas.

[0017] Further, in the technical scheme, overflow through holes can be arranged on the rotating disc to prevent liquid overflow of the mixing cylinder caused by the absorbent.

[0018] Further, in the technical scheme, a gas-liquid distribution plate can be arranged below the desulfurization unit, the gas-liquid distribution plate being fixedly installed on the wall of the spherical reactor; the gas-liquid distribution plate can be sleeved on the rotating shaft and gap-fitted with the rotating shaft, liquid overflow holes can be arranged near the position of the rotating shaft, and air holes can be uniformly and spacedly arranged on the gas-liquid distribution plate.

[0019] To achieve the above object, according to the second aspect of the present application, a desulfurization and decarburization method is provided, the desulfurization and decarburization process being completed in the same spherical reactor, and the method comprises the following steps: A, the flue gas after denitrification enters through the bottom of the reactor and is uniformly distributed in the reactor to have an upward trend; B, the rising flue gas enters the dynamic mixing cylinder and spirally rises in the cylinder under the action of rotation, reversely contacts and mixes with the SO2 absorbent from the nozzle and spirally descending in the cylinder, and performs the desulfurization process of the flue gas; C, the flue gas after desulfurization continues to rise to enter the decarburization process: through the overall rotation of the tree-shaped baffle, the CO2 absorbent from top to bottom hits the baffle, the baffle breaks the liquid into small droplets and makes the droplets spirally descend, and the descending droplets perform gas-liquid mass transfer with the flue gas after desulfurization running from bottom to top; D, the purified flue gas is discharged to the atmosphere through the gas outlet at the top of the spherical reactor.

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

[0021] Further, in the technical scheme, the CO2 absorbent can be one or more of Na2CO3, Na2SO3 and NaHCO3; and the mass concentration of the alkali solution can be 5-40%.

[0022] Further, in the technical solution, the SO2 absorbent and the CO2 absorbent can also be the same kind of double desorption absorbent, which can be one or more of NaHCO3, NH3·H2O and NaOH; on this basis, the desulfurization process of the application can simultaneously decarbonize, and the decarbonization process can simultaneously desulfurize.

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

[0024] 1) The application adopts a rotatable baffle and a through hole formed in the baffle, liquid absorbent is broken into smaller droplets during rotation, which can effectively increase the overall mass transfer rate; at the same time, part of the liquid absorbent changes its movement direction through the through hole in the baffle, and the impinged droplets are further strengthened in the spiral downward trend, the travel of the droplets is lengthened, and the droplets descend while performing gas-liquid mass transfer with the flue gas rising from below, 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 carbon dioxide absorption effect;

[0025] 2) The baffle of the adjacent layer in the overall tree-shaped decarbonization unit is provided with a deviation angle in the radial direction, and the length of the connecting rod of the lower baffle is greater than that of the upper baffle, so that the baffle can receive the impact of liquid from different directions, reducing the possibility of direct falling of the liquid, and in the overall rotating state, it is more conducive to the spiral downward of the droplets;

[0026] 3) The decarbonization unit of the tree-shaped structure, the length of each layer of connecting rods is not the same, and increases layer by layer from top to bottom, which can not only meet the spiral downward of the droplets and ensure the flue gas treatment capacity, but also fully utilize the internal space of the spherical reactor and maximize the avoidance of direct falling of the liquid entering from the nozzle to the lower space without impact;

[0027] 4) The combination of the decarbonization unit and the desulfurization unit is adopted for flue gas purification, after 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 desulfurization unit nozzle, the flow direction of the desulfurization absorbent is changed through the nozzle, and the desulfurization absorbent enters the dynamic mixing cylinder to contact with the flue gas, thereby improving the mixing uniformity of the desulfurization absorbent and the flue gas; in the rotating process of the rotating disc, the dynamic mixing cylinder can change the flow direction of the flue gas and the desulfurization absorbent, respectively showing spiral upward and downward trends, thereby enhancing the mixing and mass transfer effect and further improving the gas-liquid mass transfer rate of the desulfurization unit;

[0028] 5) The combination of the decarbonization unit and the desulfurization unit of the application can increase the gas-liquid disturbance in the mixing cylinder passage of the rotating disc of the desulfurization unit, and form a vortex in a local area, which is more conducive to gas-liquid mass transfer;

[0029] 6) The setting of the gas-liquid distribution plate below the desulfurization unit can reduce the phenomena of entrainment of mist and flooding of liquid, prolong the service life of the device, and realize long-period operation;

[0030] 7) The application adopts a new high-efficiency desulfurization and decarburization integrated process, the decarburization absorbent and the desulfurization absorbent can cooperatively remove CO2 and SO2, the two kinds of absorbents complement each other (or double desorption absorbents are used), problems such as equipment scaling and blockage caused by excessive input of absorbents are avoided; the rotating bed is used as the reactor (high-speed rotation of the rotating bed can generate a gravity field of 10-1000g), and the reactor is arranged in a spherical shape, the absorption rates of SO2 and CO2 can be ensured, the space of the spherical reactor can be fully utilized, the equipment volume is reduced, and safety and environmental protection problems are avoided; the operation flexibility of the supergravity reactor is flexible, the equipment is easy to move, and the performance is far superior to that of the traditional tower equipment.

[0031] The above description is only a summary of the technical solutions of the application, in order to more clearly understand the technical means of the application and can be implemented according to the content of the specification, at the same time, in order to make the above and other purposes, technical features and advantages of the application more easily understood, one or more preferred embodiments are listed below, and are described in detail below with reference to the drawings. BRIEF DESCRIPTION OF DRAWINGS

[0032] Figure 1 is a schematic diagram of the internal structure of the desulfurization and decarburization rotating bed device of the application (showing the structure of the desulfurization unit and the decarburization unit; the solid arrows in the figure represent the flow direction of the liquid absorbent, and the dashed arrows represent the flow direction of the flue gas).

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

[0034] Figure 3 is a schematic diagram of the baffle structure in the decarburization unit of the application.

[0035] Figure 4 is a schematic diagram of the arrangement of the absorbent pipeline and the nozzle in the desulfurization unit of the application.

[0036] Figure 5 is a top view schematic diagram of the rotating disc in the desulfurization unit of the application.

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

[0038] Figure 7 is a schematic diagram of the application of the desulfurization and decarburization rotating bed device of the application.

[0039] MAIN REFERENCE NUMERALS:

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

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

[0042] The specific embodiments of the present application will be described in detail below with reference to the accompanying drawings, but it should be understood that the scope of the present application is not limited by the specific embodiments.

[0043] Unless otherwise defined, all terms used in disclosing the application, including technical and scientific terms, have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. It will be further understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the relevant art and this application and will not be interpreted in an overly literal sense unless expressly so defined herein.

[0044] In this document, relational terms such as "first" and "second", and the like can be used solely to distinguish one entity or action from another entity or action, without necessarily requiring or implying any actual such relationship or order between such entities or actions. The terms "comprises", "comprising", or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process or method that comprises a list of steps does not include only those steps but can include other not-explicitly listed steps or elements "comprising" a recited step does not mean "consisting only of the recited step.

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

[0046] As Figure 1As shown, the present application provides a desulfurization and decarburization rotating bed device, which is a spherical reactor 100 structure, including a decarburization unit 2 and a desulfurization unit 1, which can be used for the desulfurization and decarburization of flue gas after denitrification in the same reactor. The decarburization unit 2 includes a rotating shaft 3 and a tree-shaped baffle, the rotating shaft 3 is vertically arranged in the spherical reactor 100, and a dynamic seal is arranged at the penetrating part. The tree-shaped baffle is overall tree-shaped and is circumferentially layered along the rotating shaft 3, the number of each layer of baffles 21 is multiple and is uniformly arranged, and the baffles 21 of adjacent layers are provided with a deviation angle in the radial direction. The baffle 21 is fixedly connected with the rotating shaft 3 through a connecting rod 23, and the length of the connecting rod of the lower layer baffle is greater than that of the upper layer baffle; in the rotating process of the rotating shaft 3, the CO2 absorbent impacts the baffle 21 from top to bottom, the baffle 21 breaks the liquid into fine droplets and makes the droplets spiral downward, and the downward movement is accompanied by gas-liquid mass transfer with the flue gas rising from bottom to top. Preferably but not limitedly, the baffle 21 can be provided with through holes 22 of different shapes, and the shape of the holes can be circular, square or triangular; the number of the holes is 1 to 4 and is uniformly distributed on the baffle. The design of the through hole can better change the flow direction of the liquid, the spiral downward effect of the droplet is better, and thus the gas-liquid mass transfer process is more helpful. The desulfurization unit 1 is located below the decarburization unit 2 and is used for forming the contact and mixing of the spirally rising flue gas and the spirally downward SO2 absorbent.

[0047] The decarburization unit composed of a rotatable baffle, a baffle through hole and a connecting rod in the present application is overall tree-shaped, so that the baffle 21 is basically perpendicular to the falling direction of the liquid (i.e. CO2 absorbent), the liquid can be broken into finer droplets in the rotating process, the overall mass transfer rate can be effectively increased; at the same time, the through hole 22 can further change the flow direction of the liquid, the impacted droplets spiral downward, the travel of the droplets is lengthened, the gas-liquid contact time can be effectively increased, and thus the carbon dioxide absorption effect is further improved; the baffles 21 of adjacent layers are provided with a deviation angle in the radial direction (referring to the top view of Figure 2 , and the length of the connecting rod of the lower layer baffle is greater than that of the upper layer baffle, so that the baffle 21 can accept the impact of the liquid from different directions, the possibility of direct falling of the liquid is reduced, and in the overall rotating state, the spiral downward of the droplets is more helpful; the present application sets the desulfurization unit 1 in the same spherical reactor 100 as the decarburization unit 2, so that the flue gas after denitrification realizes desulfurization and decarburization integration, which not only reduces the equipment space occupation, but also saves the investment; the desulfurization unit realizes the spiral operation of the upward flue gas and the downward SO2 absorbent, so that the gas-liquid is fully mixed and mass transferred in the limited space.

[0048] Further as shown in Figures 1 to 3 , each layer of baffles 21 has an inclination angle (i.e. inward inclination, referring to Figure 3), the inclination angle is preferably set to meet the vertical impact with the CO2 absorbent. The CO2 absorbent comes from a liquid distributor arranged at the top of the spherical reactor, i.e. a distributor arranged at the bottom of the liquid inlet 101, and the liquid sprayed from the nozzle of the distributor is distributed in the shape of an umbrella so as to better impact the baffle 21 of each layer. Due to the difference in the spray coverage angle of the nozzle and the spray travel distance, the inclination angle of the baffle can be set to decrease from top to bottom layer by layer. Further, the baffle of the uppermost layer is arranged at a position matching the height of the liquid distributor, and the baffle of the lowermost layer is arranged close to the inner wall of the spherical reactor. Since the present application adopts a spherical reactor and a decarbonization unit in the overall tree structure, the length of each layer of connecting rods 23 is not the same and increases from top to bottom layer by layer, so that the spiral downward of the mist droplets can be met, the flue gas treatment capacity is ensured, at the same time, the internal space of the spherical reactor 100 can be fully utilized, and the liquid entering from the nozzle is avoided from directly falling to the lower layer space without impact. Further, preferably but not limitedly, the cross section of the connecting rod 23 can be designed to be flat, so that the connecting rod itself can also accept the impact of the liquid, thereby better realizing the atomization effect. One end of the connecting rod 23 is fixedly connected with the baffle 21, and the other end is fixedly connected with the rotating shaft 3, so that each baffle 21 of the layer can rotate with the rotating shaft 3. Specifically, according to the size of the inner diameter of the spherical reactor, the baffle is preferably arranged in 5 to 10 layers, the deviation angle of each layer is 5° to 15°, and each layer of baffles can be arranged in 4 and arranged in the shape of a cross (see Figure 2 ).

[0049] Further as shown in Figure 1 、 4 , 5, the desulfurization unit 1 of the present application at least includes a nozzle 11 and a dynamic mixing cylinder 13. The nozzle 11 is arranged below the decarbonization unit 2 and communicates with the absorbent pipeline 12, and the nozzle is fixed and arranged as a static nozzle. The dynamic mixing cylinder 13 is arranged below the nozzle 11 and corresponds to the position of the nozzle, and the dynamic mixing cylinder 13 is a cylinder structure with both ends open, and the lower end is fixedly connected with the rotating disc 4, and the rotating disc 4 can rotate with the rotating shaft 3. The flue gas rising in the dynamic mixing cylinder 13 spirally rises under the action of the rotating disc, and the SO2 absorbent from the nozzle spirally descends after entering the mixing cylinder. Specifically, referring to Figure 4, the nozzle 11 is arranged on the absorbent pipeline 12, 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 with the rotating disc 4, when the rotating disc 4 rotates at high speed with the rotating shaft 3, the upward flue gas in the mixing cylinder presents a spiral upward trend, the downward SO2 absorbent presents a spiral downward trend, the gas-liquid contact time is longer, the mixing and mass transfer are more sufficient, the rotating disc 4 is provided with 2-6 overflow holes 14, for preventing liquid from flooding the dynamic mixing cylinder 13 and causing liquid overflow. The desulfurization unit composed of the nozzle 11, the dynamic mixing cylinder 13 and the rotating disc 4 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 present a spiral downward and upward trend, accelerates the mixing, enhances the mixing and mass transfer effect, and further improves the utilization rate of the SO2 absorbent. The inventor has proved through experiments that, by adopting the setting mode that the dynamic mixing cylinder is matched with the static nozzle, the gas-liquid mass transfer efficiency of the SO2 absorbent and the flue gas is higher.

[0050] Further referring to Figure 4 , the absorbent pipelines 12 are 2-4 in the vertical direction (i.e. Figure 4 in the vertical direction) and 2-4 in the horizontal direction (i.e. Figure 4 in the horizontal direction), 4-10 nozzles 11 are arranged on each absorbent pipeline, and the number of pipelines and nozzles is determined according to the actual SO2 content in the flue gas. Figure 5 Further referring to

[0051] Further as shown in Figure 1 and 6 , the gas-liquid distribution plate 5 can also be arranged below the desulfurization unit 1, the gas-liquid distribution plate 5 is fixedly installed 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 gap cooperation with the rotating shaft 3, the liquid overflow hole 52 (two are arranged in the Figure 6 ) is arranged at the position close to the rotating shaft 3, and the air vent hole 51 is also uniformly and interval arranged on the gas-liquid distribution plate 5. The added gas-liquid distribution plate can reduce the entrainment phenomenon of the existing rotating bed, prolong the operation life of the device, and realize long-period operation.

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

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

[0054] Step S102, the rising flue gas enters the dynamic mixing cylinder 13 and under the action of rotation, it is in a spiral upward state in the cylinder, and is in reverse contact and mixing with the SO2 absorbent from the nozzle and entering the cylinder in a spiral downward state, to perform the desulfurization process of the flue gas. The SO2 absorbent can use one or more of CaO, Ca(OH)2, CaCO3, Na2CO3, NaOH, KOH, NH3, NH4OH and NH4HCO3; the mass concentration of the alkali solution is 5-40%.

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

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

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

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

[0059] The flue gas after denitration by the denitration device 200 passes through the denitration outlet flue gas pipeline 201 into the flue gas heat exchanger 400 and exchanges heat with low-temperature steam, and then enters the spherical reactor 100. After the flue gas in the spherical reactor 100 undergoes the foregoing desulfurization and decarburization process, the flue gas leaves the reactor through the gas outlet 102 at the top of the reactor. The liquid (alkali liquor can be used) as the desulfurization and decarburization absorbent enters the reactor from the top and middle absorbent pipelines (pumped by the decarburization absorbent inlet pump 501 and the desulfurization absorbent inlet pump 502, respectively), is sprayed out through the nozzles to form an umbrella-shaped distribution, and then undergoes gas-liquid mass transfer in the tree-shaped decarburization unit 2 and the desulfurization unit 1 to remove sulfur dioxide and carbon dioxide in the flue gas (double-removal absorbent is used). Finally, the two kinds of absorbents are collected at the bottom of the reactor and then led out by the liquid discharge pipe to the absorbent outlet pump 503, enter the lean-liquid heat exchanger 500, and then enter the upper part of the regeneration tower 300 to undergo the absorbent regeneration process. The lean-liquid absorbent after regeneration leaves the bottom of the regeneration tower 300, enters the lean-liquid heat exchanger 500, and then enters the decarburization 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 method of the present application. The denitration outlet flue gas flow is 100,000 cubic meters per hour, the sulfur dioxide concentration in the flue gas is 800 mg / Nm 3 , the carbon dioxide concentration is 15%, the flow rate is 12 m / s, the temperature is 180°C, sodium bicarbonate solution is used as the decarburization absorbent, and sodium hydroxide is used as the desulfurization absorbent. The tree-shaped decarburization unit has 9 layers, each layer has 4 cross-shaped baffles, each baffle has 4 through holes, the rotating disc of the desulfurization unit rotates at a speed of about 800 r / min, there are 2 north-south and 2 east-west absorbent pipelines, each absorbent pipeline is provided with 6 nozzles, and 6 dynamic mixing cylinders are arranged along the radial direction of the rotating disc and are uniformly arranged on the two diameters.

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

[0063] According to the calculation, 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] The device and process method are used in a certain catalytic cracking system, the flow of flue gas at the denitration outlet is 120,000 cubic meters per hour, the concentration of sulfur dioxide in the flue gas is 800 mg / Nm 3 , the concentration of carbon dioxide is 15%, the flow rate is 12 m / s, and the temperature is 180℃, and sodium bicarbonate solution is used as the absorbent. The tree-shaped decarbonization unit has 9 layers, each layer has 4 baffles arranged in a cross shape, each baffle has 4 through holes, the rotating disc of the desulfurization unit rotates at a speed of about 800 r / min, there are 2 north-south and 2 east-west absorbent pipelines, each absorbent pipeline is provided with 6 nozzles, and 6 dynamic mixing cylinders are arranged along the radial direction of the rotating disc and uniformly arranged on the two diameters.

[0066] The flue gas (180℃) at the denitration outlet enters the flue gas heat exchanger and exchanges heat with low-temperature steam (40℃), and then enters the spherical reactor, the flue gas passes through the desulfurization and decarbonization units, and then leaves the reactor through the top of the reactor. The sodium bicarbonate solution enters the reactor through the top and middle absorbent pipelines, the flue gas and the sodium bicarbonate solution complete two gas-liquid mass transfer in the decarbonization unit and the desulfurization unit, remove sulfur dioxide and carbon dioxide in the flue gas, and finally gather at the bottom of the reactor and are introduced to the absorbent outlet pump through the liquid discharge pipe, enter the regenerator through the lean-lean heat exchanger, and then the absorbent regeneration process is carried out, the regenerated absorbent leaves the regenerator from the bottom and enters the lean-lean heat exchanger, and then enters the decarbonization absorbent inlet pump and the desulfurization absorbent inlet pump and returns to the spherical reactor through the liquid inlet pipe.

[0067] According to calculation, the removal rates of sulfur dioxide and carbon dioxide are 98% and 85%, respectively, and the utilization rate of the absorbent is 85%, and the overall equipment occupies an area reduced by 50%.

[0068] Comparative Example Comparative Example

[0069] A traditional wet desulfurization device is added with a traditional carbon capture device for decarbonization treatment. The flow of flue gas at the denitration outlet is 120,000 cubic meters per hour, the concentration of sulfur dioxide in the flue gas is 800 mg / Nm 3 , the concentration of carbon dioxide is 15%, the flow rate is 12 m / s, and the temperature is 180℃, and sodium bicarbonate solution is used as the decarbonization absorbent, and sodium hydroxide is used as the desulfurization absorbent.

[0070] The flue gas (180℃) at the denitration outlet directly enters the wet desulfurization tower, the flue gas after desulfurization (60℃) enters the carbon capture device, and finally leaves the device through the flue gas outlet pipe. The sodium bicarbonate solution enters through the liquid inlet pipe and is introduced through the liquid discharge pipe, enters the upper part of the regenerator through the lean-lean heat exchanger, and then the absorbent regeneration process is carried out, the regenerated sodium bicarbonate leaves the regenerator from the bottom and enters the lean-lean heat exchanger, and then is pumped and returned to the carbon capture device through the liquid inlet pipe.

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

[0072] The foregoing description of specific exemplary embodiments of the application has been presented for the purposes of illustration and description. It is not intended to be exhaustive or to limit the application to the precise forms disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain the principles of the application and its practical application, to thereby enable others skilled in the art to best utilize the application and various embodiments with various modifications as are suited to the particular use contemplated. Any simple modification, equivalent replacement, and modification of the above-described exemplary embodiments should fall within the scope of the application.

Claims

1. A desulfurization and decarburization rotating bed device, characterized by, The spherical reactor structure comprises: a decarburization unit comprising a rotating shaft vertically penetrating in the spherical reactor and a tree-shaped baffle, the tree-shaped baffle is integrally tree-shaped and is arranged in layers along the circumference of the rotating shaft, the number of baffles in each layer is multiple and is uniformly arranged, the baffles of adjacent layers are radially arranged with a deviation angle, the baffles are fixedly connected with the rotating shaft through connecting rods, the length of the connecting rods of the lower layer baffles is greater than that of the upper layer baffles, in the rotating process of the rotating shaft, the CO2 absorbent hits the baffles from top to bottom, the baffles break the liquid into fine droplets and make the droplets spiral downward, while descending, the droplets contact and mass transfer with the flue gas ascending from bottom to top; a desulfurization unit located below the decarburization unit, for forming contact and mixing of the spiral ascending flue gas and the spiral descending SO2 absorbent.

2. The desulfurization and decarburization rotating bed apparatus according to claim 1, characterized by, Each layer of the baffles has an inclination angle, the inclination angle meets the vertical impact of the CO2 absorbent, the CO2 absorbent comes from a liquid distributor arranged at the top of the spherical reactor.

3. The desulfurizing and decarburizing rotating bed apparatus according to claim 2, wherein The inclination angle of the baffles decreases layer by layer from top to bottom.

4. The desulfurizing and decarburizing rotating bed apparatus according to claim 3, wherein The arrangement position of the uppermost layer of the baffles is matched with the height of the liquid distributor, the arrangement position of the lowermost layer of the baffles is close to the inner wall of the spherical reactor.

5. The desulfurizing and decarburizing rotating bed apparatus according to claim 1, wherein The cross section of the connecting rod is flat, one end of the connecting rod is fixedly connected with the baffle, the other end of the connecting rod is fixedly connected with the rotating shaft.

6. The decarbonizing and decarburizing rotating bed apparatus according to claim 1, wherein The baffles are arranged in 5 to 10 layers, the deviation angle of each layer is 5° to 15°, the number of baffles in each layer is 4.

7. The decarbonization and decarbonization rotating bed apparatus according to claim 1, characterized by The baffle is provided with holes, the shape of the holes is circular, square or triangular, the number of the holes is 1 to 4 and is uniformly distributed on the baffle.

8. The decarbonization and decarbonization rotating bed apparatus according to claim 1, characterized by The desulfurization unit comprises: a nozzle arranged below the decarburization unit and communicated with an absorbent pipeline, the nozzle is fixed; a dynamic mixing cylinder arranged below the nozzle and corresponding to the position of the nozzle, the dynamic mixing cylinder is a cylindrical structure with open two ends, and the lower end is fixedly connected with a rotating disc, the rotating disc rotates with the rotating shaft, the flue gas ascending in the mixing cylinder spirally ascends under the action of rotation, the SO2 absorbent from the nozzle spirally descends after entering the mixing cylinder.

9. The desulfurizing and decarburizing rotating bed apparatus according to claim 8, wherein The absorbent pipeline extends along the horizontal direction and the number of the absorbent pipelines is multiple, the absorbent pipelines and the nozzle are uniformly distributed and the number of the absorbent pipelines is determined according to the SO2 content in the flue gas.

10. The desulfurizing and decarburizing rotating bed apparatus according to claim 8, wherein Overflow through holes are arranged on the rotating disc to prevent liquid overflow caused by absorbent flooding the mixing cylinder.

11. The desulfurizing and decarburizing rotating bed apparatus according to claim 8, characterized by A gas-liquid distribution plate is arranged below the desulfurization unit, 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 gap-fitted with the rotating shaft, liquid overflow holes are arranged close to the rotating shaft, and air holes are uniformly and interval arranged on the gas-liquid distribution plate.

12. A desulfurization and decarburization method characterized by, The desulfurization and decarburization process is 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 uniformly distributed in the reactor to ascend; B, the ascending flue gas enters the dynamic mixing cylinder and spirally ascends in the cylinder under the action of rotation, reversely contacts and mixes with the SO2 absorbent from the nozzle and spirally descending in the cylinder, and performs the desulfurization process of the flue gas; C. The flue gas after desulfurization continues to rise into the decarburization process: through the overall rotation of the tree-shaped baffle, the CO2 absorbent hits the baffle from top to bottom, the baffle breaks the liquid into fine droplets and makes the droplets spiral downward, while descending, the flue gas after desulfurization running from bottom to top carries out gas-liquid mass transfer; D. The purified flue gas is discharged to the atmosphere through the gas outlet at the top of the spherical reactor.

13. The desulfurization and decarburization method according to claim 12, characterized by, 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 alkali solution is 5-40%.

14. The desulfurization and decarburization method according to claim 12, characterized by, The CO2 absorbent is one or more of Na2CO3, Na2SO3 and NaHCO3; the mass concentration of the alkali solution is 5-40%.

15. The desulfurization and decarburization method according to claim 12, characterized by, The SO2 absorbent and the CO2 absorbent use the same double desorption absorbent, which is one or more of NaHCO3, NH3·H2O and NaOH; on this basis, the desulfurization process simultaneously decarburizes, and the decarburization process simultaneously desulfurizes.

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