Vertical gas inlet supergravity sulfur dioxide absorption device and sulfur dioxide gas absorption treatment method

Abstract

The invention relates to the technical field of sulfur dioxide flue gas treatment, and particularly discloses a vertical gas inlet supergravity sulfur dioxide absorption device which comprises a kettle body, a stirring assembly, a feeding assembly and a gas inlet piece, the stirring assembly comprises a stirring shaft and a driving part connected with the stirring shaft, and one end of the stirring shaft extends into the kettle body; the feeding assembly comprises a feeding pipe and material distribution discs, the material distribution discs are installed on the stirring shaft in the kettle body and distributed along the stirring shaft at intervals, the material distribution discs are connected with the feeding pipe, and a plurality of discharging ports are formed in the material distribution discs in the circumferential direction; the air inlet direction of the air inlet piece is perpendicular to the discharging direction of the material distribution disc. According to the invention, through coupling of a vertical gas inlet mode and a supergravity technology, a material liquid forms an extremely thin liquid film in a supergravity field under the action of a material distribution disc, the liquid film is cut into micron-sized liquid drops by a gas phase at the moment of flying out of the outer edge of the material distribution disc, the mass transfer process is greatly enhanced, and the desulfurization efficiency is higher than gt; and the device is small in size, low in pressure drop and not easy to block.

Description

Technical Field

[0001] This invention relates to the field of sulfur dioxide flue gas treatment technology, specifically to a vertically inlet supergravity sulfur dioxide absorption device and a method for absorbing and treating sulfur dioxide gas. Background Technology

[0002] Sulfur dioxide is an air pollutant, and its emission control is crucial. Currently, wet desulfurization methods, such as the limestone-gypsum method and manganese dioxide ore method used in flue gas desulfurization, are the most widely used technologies for sulfur dioxide treatment. However, the core equipment of these technologies, the absorption tower, is bulky, occupies a large area, and has limited mass transfer efficiency.

[0003] To overcome the shortcomings of traditional equipment such as absorption towers, hypergravity technology has emerged. It generates a hypergravity field through high-speed rotating liquid, breaking the liquid into micron-sized droplets or extremely thin films, greatly enhancing the mass transfer process. However, most existing hypergravity devices use axial gas intake, which leads to problems in practical applications such as uneven gas distribution, short gas residence time in the packing layer, low mass transfer efficiency, and large pressure drop, requiring urgent improvement.

[0004] Chinese Patent Application No. 201910968932.8 discloses a continuous production system and method for sulfonates using a coupled reaction separation and absorption process, wherein the supergravity device cuts the raw material oil into liquid films and droplets, utilizing a high-speed rotating packing to cut the raw material. Chinese Patent Application No. 202111498938.7 discloses a device and method for simultaneous desulfurization and denitrification of coal-fired flue gas, utilizing a perforated packing to cut the liquid. However, these supergravity devices and traditional supergravity equipment are designed for two-phase gas-liquid processing, and are not applicable to three-phase gas-solid-liquid processes involving solids. Therefore, developing a supergravity absorption device adapted to three-phase gas-solid-liquid processing to further optimize airflow organization, reduce energy consumption, and improve desulfurization efficiency is a key challenge and focus of research in this field. Summary of the Invention

[0005] The technical problem solved by this invention is to provide a vertically inlet supergravity sulfur dioxide absorption device and a sulfur dioxide gas absorption and treatment method, so as to solve the problem that existing supergravity devices cannot adapt to gas-solid-liquid three-phase treatment, and further optimize airflow organization, reduce energy consumption, and improve desulfurization efficiency.

[0006] The technical problem solved by this invention is achieved by the following technical solution: A vertically inlet supergravity sulfur dioxide absorption device includes a vessel body, a stirring assembly, a feeding assembly, and an air inlet component. The stirring assembly includes a stirring shaft and a drive component connected to the stirring shaft, with one end of the stirring shaft extending into the vessel body. The feeding assembly includes a feeding pipe and a distribution plate. The distribution plate is installed on the stirring shaft inside the vessel body and is spaced apart along the stirring shaft. The distribution plate is connected to the feeding pipe, and multiple discharge ports are arranged circumferentially on the distribution plate. The air inlet direction of the air inlet component is perpendicular to the discharge direction of the distribution plate.

[0007] Furthermore, the distribution plate has a shaft hole at its center, and a feed ring groove is provided outside the shaft hole. The feed pipe is sleeved in the feed ring groove and does not rotate with the distribution plate.

[0008] Furthermore, the material distribution plate is provided with multiple material distribution chambers that communicate with the feed ring groove. The multiple material distribution chambers are separated by guide plates, and the material distribution chambers are provided with discharge ports on the outside.

[0009] Furthermore, the guide vane is an S-shaped guide vane.

[0010] Furthermore, the air intake direction of the air intake pipe is parallel to the length direction of the stirring shaft, and the discharge direction of the material distribution plate is arranged perpendicular to the stirring shaft.

[0011] Furthermore, the feeding assembly includes at least four distribution discs spaced apart along the stirring shaft, each distribution disc being provided with at least one matching feed pipe.

[0012] Furthermore, the air intake component includes an air intake pipe connected to the material distribution plate, and an exhaust port is also provided on the reactor body. The air intake pipe and the exhaust port are respectively located on both sides of the feeding assembly.

[0013] Furthermore, a drain port is provided at the bottom of the vessel body, which is connected to a return liquid storage tank. The return liquid storage tank is connected to the feed pipe via a circulation pump, and a feed port is provided on the return liquid storage tank.

[0014] Furthermore, the driving component is a drive motor, which is located outside the vessel body. A bearing housing is located outside the stirring shaft, and the drive motor and the bearing housing are connected by a coupling. A bearing seat is located at the tail end of the vessel body.

[0015] A method for absorbing and treating sulfur dioxide gas, using the supergravity sulfur dioxide absorption device described above.

[0016] Further, the processing method is as follows: the liquid material is fed into the distribution plate through the feed pipe, and the flue gas containing sulfur dioxide is fed into the reactor through the air inlet; the air inlet direction of the air inlet is arranged perpendicular to the discharge direction of the distribution plate; the liquid material is a manganese sulfate solution containing manganese dioxide particles or a calcium carbonate aqueous solution containing manganese dioxide particles. The liquid material forms multiple thin liquid films under the action of multiple spaced distribution plates, and the liquid material is cut into micron-sized droplets by the vertically input flue gas containing sulfur dioxide at the moment it is thrown out of the distribution plate, and then continues to carry out a gas-liquid-solid three-phase reaction in the reactor; the liquid material at the bottom of the reactor enters the return liquid storage tank with a stirring mechanism and is then connected to the feed pipe through a circulation pump; the gas after the reaction in the reactor is completed is discharged through the exhaust port at the top of the reactor.

[0017] Preferably, the Baumé degree of the feed liquid in the feed pipe is 30-45, the pH value of the feed liquid is 0.5-2, and the solid content of manganese dioxide particles in the feed liquid is 10-15%.

[0018] Preferably, the circulation flow rate of the circulating pump is 80~120m³. 3 / h.

[0019] Preferably, the air intake volume of the air intake component is 14000~16000 m³. 3 / h, the sulfur dioxide concentration in the flue gas is 21000~25000 mg / m³ 3 .

[0020] Preferably, the reaction temperature of the liquid material in the reactor is 45~90℃.

[0021] Preferably, when the solid content of manganese dioxide particles in the liquid at the outlet of the circulating pump is 2-5%, new slurry is added.

[0022] Preferably, the sulfur dioxide concentration in the exhaust gas is less than 30 mg / m³. 3 Dust concentration < 0 mg / m³ 3 .

[0023] Beneficial Effects: The vertical air intake supergravity sulfur dioxide absorption device of this invention couples vertical air intake with supergravity technology. The device generates a supergravity field through high-speed rotating liquid material. Under the action of the distribution plate within the supergravity field, the liquid material forms an extremely thin liquid film. The air intake direction of the air intake component is arranged perpendicular to the discharge direction of the distribution plate. Therefore, the liquid film is cut into micron-sized droplets by the gas phase the instant it flies out of the outer edge of the distribution plate, greatly enhancing the mass transfer process. The desulfurization efficiency of this invention is higher than 99.5%, and the device is small in size, has low pressure drop, and is not easily clogged. Therefore, it is particularly suitable for the gas-solid-liquid three-phase reaction of liquid material containing solid particles with sulfur dioxide gas, and is suitable for installation in confined spaces and industrial flue gas treatment.

[0024] The sulfur dioxide gas absorption and treatment method of this invention involves the reaction of sulfur dioxide in flue gas with water in a feed solution to produce sulfuric acid, which then reacts with manganese dioxide particles in the feed solution to produce manganese sulfate. The flue gas after sulfur dioxide absorption is discharged through an exhaust port, and the reacted feed solution can be recycled. This invention couples a vertical air intake method with hypergravity technology and utilizes sufficient three-phase contact and reaction to ensure that the sulfur dioxide concentration in the treated flue gas is less than 30 mg / m³. 3 Dust concentration <30mg / m³ 3 It has high desulfurization efficiency and low energy consumption, and has a promising application prospect. Attached Figure Description

[0025] Figure 1 This is a schematic diagram of the supergravity sulfur dioxide absorption device in Embodiment 1 of the present invention.

[0026] Figure 2 for Figure 1 A schematic diagram of the structure of the center-divided tray.

[0027] Figure 3 This is a schematic diagram of the structure of the supergravity sulfur dioxide absorption device in Embodiment 2 of the present invention.

[0028] The components are as follows: 1. Kettle body; 2. Feeding assembly; 21. Distribution plate; 211. Distribution chamber; 212. Discharge port; 213. Shaft hole; 214. Guide vane; 215. Feeding ring groove; 22. Feeding pipe; 3. Air inlet; 4. Stirring assembly; 41. Drive motor; 42. Coupling; 43. Stirring shaft; 44. Bearing housing; 45. Seal; 46. Bearing seat; 5. Exhaust port; 6. Drain port; 7. Manhole. Detailed Implementation

[0029] To make the technical means, creative features, objectives and effects of this invention easier to understand, the invention will be further described below with reference to specific embodiments.

[0030] Example 1 like Figure 1 and Figure 2 As shown, a vertically inlet supergravity sulfur dioxide absorption device includes a horizontal vessel body 1, a stirring assembly 4, a feeding assembly 2, and an air inlet component 3.

[0031] The vessel body 1 is provided with a manhole 7 to facilitate real-time observation of the operation inside the vessel body 1. The bottom of the vessel body 1 is provided with a drain port 6, through which the liquid after the reaction is completed is discharged.

[0032] The stirring assembly 4 includes a stirring shaft 43 and a driving component connected to the stirring shaft 43. One end of the stirring shaft 43 extends into the vessel body 1. The driving component is a drive motor 41, which is located outside the vessel body 1. A bearing housing 44 is located outside the stirring shaft 43. The drive motor 41 and the bearing housing 44 are connected by a coupling 42. A bearing seat 46 is provided at the tail of the vessel body 1 to ensure the stable operation of the rotating shaft.

[0033] The feeding assembly 2 includes a feeding pipe 22 and a distributing disc 21. The distributing disc 21 is installed on the stirring shaft 43 inside the vessel body 1 and is distributed at intervals along the stirring shaft 43. In this embodiment, it includes four distributing discs 21 arranged at intervals. During feeding, the four distributing discs 21 form four parallel liquid films in the opposite direction along the extension of the stirring shaft 43. Each distributing disc 21 is provided with a matching feeding pipe 22. The center of the distributing disc 21 is provided with a shaft hole 213, which allows the stirring shaft 43 to pass through. A feeding ring groove 215 is provided outside the shaft hole 213, and the feeding pipe 22 is sleeved in the feeding ring groove 215. The distributing disc 21 is fixedly connected to the stirring shaft 43 and rotates with the rotation of the stirring shaft 43. When the distributing disc 21 rotates, the feeding pipe 22 supplies liquid to the distributing disc 21 but does not rotate with the distributing disc 21.

[0034] like Figure 3 As shown, the distributing disc 21 also includes multiple distributing chambers 211 disposed inside the distributing component. These chambers are separated by guide vanes 214, preferably S-shaped. The S-shaped vanes reduce friction within the distributing chambers 211 and allow the solution to tangentially eject, forming a liquid film. The distributing chambers 211 communicate with the inlet ring groove 215. The outer side of the distributing chamber 211 away from the inlet ring groove 215 is the outlet 212. The distributing disc 21 contains multiple distributing chambers 211, meaning multiple outlets 212 are arranged circumferentially on the side of the distributing disc 21. The air intake direction of the air inlet component 3 is perpendicular to the discharge direction of the distributing disc 21. Specifically, the discharge direction of the distributing disc 21 is perpendicular to the stirring shaft 43, and the air intake direction of the air inlet pipe is parallel to the length direction of the stirring shaft 43.

[0035] In this invention, the drain port 6 is connected to the return liquid storage tank (not shown in the figure). The return liquid storage tank is connected to the plurality of feed pipes 22 through a circulation pump. The return liquid storage tank is provided with a feed port for adding new liquid to adjust the solid content of the liquid in the return liquid storage tank.

[0036] The vessel body 1 is also provided with an exhaust port 5, and the air inlet pipe and the exhaust port 5 are respectively located on both sides of the feeding assembly 2.

[0037] In practical applications, the air inlet direction is perpendicular to the liquid film direction. SO2-containing flue gas enters the high-speed rotating liquid film bed along the axial direction, that is, perpendicular to the distribution plate 21. The liquid material enters the distribution plate 21 through the feed pipe 22 and is divided by the distribution plate 21. The distribution plate 21 rotates at high speed with the stirring shaft 43, and the rotation speed of the distribution plate 21 can be freely adjusted within the range of 100~2000 rpm. Under a hypergravity field, the liquid material is broken into micron-sized droplets or extremely thin liquid films, which efficiently counter-current or cross-current with the radially passing flue gas. This greatly increases the contact opportunities between sulfur dioxide molecules and the liquid material such as calcium carbonate and manganese dioxide, significantly enhancing the gas-liquid mass transfer process. The desulfurization efficiency of the sulfur dioxide flue gas is higher than 99.5%.

[0038] A method for absorbing and treating sulfur dioxide gas, using the supergravity sulfur dioxide absorption device described in this embodiment; the treatment method is as follows: A feed liquid is fed into a distribution plate through a feed pipe. Preferably, the Baume degree of the feed liquid is 30-45, the pH value is 0.5-2, and the solid content of manganese dioxide particles in the feed liquid is 10-15%. In this embodiment, the Baume degree of the feed liquid is 40, the pH value is approximately 1.5, and the solid content of manganese dioxide particles in the feed liquid is 12%. Sulfur dioxide-containing flue gas is then fed into the reactor through an air inlet, with an air intake rate of 14000-16000 m³ / h. 3 / h, the sulfur dioxide concentration in the flue gas is 21000~25000 mg / m³ 3 In this embodiment, the air intake volume of the air intake component is 15000 m³. 3 / h, the sulfur dioxide concentration in the flue gas is 22000 mg / m³ 3 The air intake direction of the air inlet is perpendicular to the discharge direction of the distribution plate; the liquid material forms multiple thin liquid films under the action of multiple spaced distribution plates, and the liquid material is cut into micron-sized droplets by the vertically input sulfur dioxide-containing flue gas at the moment of discharge, and continues to undergo a gas-liquid-solid three-phase reaction in the reactor body at a reaction temperature of 50°C; the liquid material at the bottom of the reactor body is connected to the feed pipe through a circulation pump, preferably, the circulation flow rate of the circulation pump is 80~120m³ / h. 3 / h, in this embodiment, the circulation flow rate of the circulating pump is 100m³ / h. 3 In actual operation, when the solid content of manganese dioxide particles in the liquid at the outlet of the circulating pump is 4%, new slurry is added to bring the solid content of manganese dioxide particles in the liquid in the feed pipe to 12%. The gas produced after the reaction in the reactor is completed is discharged through the exhaust port at the top of the reactor. Testing shows that during operation, the concentration of sulfur dioxide in the gas discharged through the exhaust port is less than 30 mg / m³. 3 Dust concentration <30mg / m³ 3 .

[0039] Example 2 The vessel body described in this embodiment is a vertical vessel body. The stirring assembly described in this embodiment does not require a bearing seat. The rest is the same as in Embodiment 1.

[0040] The sulfur dioxide gas absorption and treatment method described in this embodiment uses the supergravity sulfur dioxide absorption device described in this embodiment. The treatment method is as follows: A liquid feed is introduced into the distribution plate through the feed pipe. Preferably, the Baume degree of the liquid feed is 30-45, the pH value is 0.5-2, and the solid content of manganese dioxide particles in the liquid feed is 10-15%. In this embodiment, the Baume degree of the liquid feed is 35, the pH value is approximately 1.8, and the solid content of manganese dioxide particles in the liquid feed is 10%. Sulfur dioxide-containing flue gas is then introduced into the reactor through an air inlet, with an air intake rate of 14000-16000 m³ / h. 3 / h, the sulfur dioxide concentration in the flue gas is 21000~25000 mg / m³ 3 In this embodiment, the air intake volume of the air intake component is 14000 m³. 3 / h, the sulfur dioxide concentration in the flue gas is 21000 mg / m³ 3 The air intake direction of the air inlet is perpendicular to the discharge direction of the distribution plate; the liquid material forms multiple thin liquid films under the action of multiple spaced distribution plates, and the liquid material is cut into micron-sized droplets by the vertically input sulfur dioxide-containing flue gas at the moment of discharge, and then continues to undergo a gas-liquid-solid three-phase reaction in the reactor body at a reaction temperature of 60°C; the liquid material at the bottom of the reactor body is connected to the feed pipe through a circulation pump, preferably, the circulation flow rate of the circulation pump is 80~120m³. 3 / h, in this embodiment, the circulation flow rate of the circulating pump is 100m³ / h. 3 In actual operation, when the solid content of manganese dioxide particles in the liquid at the outlet of the circulating pump is 4%, new slurry is added to bring the solid content of manganese dioxide particles in the liquid in the feed pipe to 10%. The gas produced after the reaction in the reactor is completed is discharged through the exhaust port at the top of the reactor. Testing shows that during operation, the concentration of sulfur dioxide in the gas discharged through the exhaust port is less than 30 mg / m³. 3 Dust concentration <30mg / m³ 3 .

[0041] The foregoing has shown and described the basic principles, main features, and advantages of the present invention. Those skilled in the art should understand that the present invention is not limited to the above embodiments. The embodiments and descriptions in the specification are merely illustrative of the principles of the invention. Various changes and modifications can be made to the invention without departing from its spirit and scope, and all such changes and modifications fall within the scope of the present invention as claimed. The scope of protection of the present invention is defined by the appended claims and their equivalents.

Claims

1. A vertical intake hypergravity sulfur dioxide absorption device, characterized by, The application relates to a high-gravity sulfur dioxide absorption device, which comprises a kettle body, a stirring assembly, a feeding assembly and an air inlet part; the stirring assembly comprises a stirring shaft and a driving part connected with the stirring shaft, and the stirring shaft extends into the kettle body at one end; the feeding assembly comprises a feeding pipe and a distribution disc, the distribution disc is installed on the stirring shaft in the kettle body and is distributed at intervals along the stirring shaft, the distribution disc is connected with the feeding pipe, and a plurality of discharge ports are arranged on the distribution disc in the circumferential direction; and the air inlet direction of the air inlet part is perpendicular to the discharge direction of the distribution disc.

2. The vertical gas entry hypergravity sulfur dioxide absorption apparatus according to claim 1, characterized by, The distribution disc is provided with a shaft hole in the center, an outer part of the shaft hole is provided with a feeding ring groove, the feeding pipe is sleeved in the feeding ring groove, and the feeding pipe does not rotate with the distribution disc.

3. The vertical air sparged hydrotrapping apparatus for sulfur dioxide according to claim 2, wherein The distribution disc is internally provided with a plurality of distribution cavities which are communicated with the feeding ring groove, the distribution cavities are separated by flow guide pieces, and the outer sides of the distribution cavities are provided with the discharge ports.

4. The vertical gas entry hypergravity sulfur dioxide absorption apparatus according to claim 2, wherein The flow guide piece is an S-shaped flow guide piece.

5. The vertical air sparged hydrotrapping apparatus for sulfur dioxide according to claim 1, wherein The air inlet direction of the air inlet pipe is parallel to the length direction of the stirring shaft, and the discharge direction of the distribution disc is arranged perpendicularly to the stirring shaft.

6. The vertical air sparged hydrotrapping apparatus for sulfur dioxide according to claim 1, wherein The feeding assembly comprises at least four distribution discs which are distributed at intervals along the stirring shaft, and each distribution disc is provided with at least one matched feeding pipe.

7. The vertical air sparged hydrotrapping apparatus for sulfur dioxide according to claim 1, wherein The air inlet part comprises an air inlet pipe which is connected with the distribution disc, the kettle body is further provided with an exhaust port, and the air inlet pipe and the exhaust port are separately arranged on the two sides of the feeding assembly.

8. The vertical air sparged hydrotrapping apparatus for sulfur dioxide according to claim 1, wherein The kettle body is provided with a liquid discharge port at the bottom, the liquid discharge port is connected with a liquid return storage tank, the liquid return storage tank is connected with the feeding pipe through a circulating pump, and the liquid return storage tank is provided with a feeding opening.

9. The vertical air sparged hydrotrapping apparatus for sulfur dioxide according to claim 1, wherein The driving part is a driving motor, the driving motor is arranged outside the kettle body, a bearing box is arranged outside the stirring shaft, the driving motor and the bearing box are connected through a shaft coupling, and a bearing seat is arranged at the tail of the kettle body.

10. A sulfur dioxide gas absorption treatment method characterized by, The high-gravity sulfur dioxide absorption device is used for processing, a feeding pipe is used for feeding liquid into the distribution disc, an air inlet part is used for feeding flue gas containing sulfur dioxide into the kettle body, the air inlet direction of the air inlet part is arranged perpendicularly to the discharge direction of the distribution disc, the liquid is manganese sulfate solution containing manganese dioxide particles or calcium carbonate aqueous solution, the liquid forms multiple thin liquid films under the action of the multiple distribution discs arranged at intervals, the liquid is cut into micron-level liquid drops by the perpendicularly input flue gas containing sulfur dioxide at the moment of being thrown out by the distribution disc, and then the liquid drops continue to carry out gas-liquid-solid three-phase reaction in the kettle body, the liquid at the bottom of the kettle body enters a liquid return storage tank with a stirring mechanism, and then the liquid is connected with the feeding pipe through a circulating pump, and the gas in the kettle body is discharged through an exhaust port at the top of the kettle body after reaction.

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