A kind of absorption reaction device for reducing leaching of manganese ore by sulfur dioxide

Abstract

The utility model discloses absorption reaction devices of sulfur dioxide reduction leaching manganese ore, including absorption tower and circulating tank, the absorption tower includes tower body, sets up the exhaust pipe at tower body top, sets up the first liquid discharge pipe at tower body bottom or lower part, sets up first reactor, second reactor and third reactor in proper order from top to bottom in tower body, first reactor connects feed pipe, second reactor and third reactor are connected circulating tank through slurry backflow pipe respectively, set up air hole on first reactor and second reactor, circulating tank is connected with absorption tower through first liquid discharge pipe, still sets up air inlet pipe, air outlet pipe and second liquid discharge pipe on circulating tank, air inlet pipe is used for supplying sulfur dioxide original gas to circulating tank, air outlet pipe passes through tower body and is connected with the air inlet of third reactor, the utility model discloses simple structure, operation and maintenance simple, sulfur dioxide absorption efficiency is high, tail gas emission is low, has good popularization and application value.

Description

Technical Field

[0001] This utility model relates to the technical field of manganese sulfate production equipment, specifically to an absorption reaction device for reducing and leaching manganese ore with sulfur dioxide. Background Technology

[0002] The wet reduction leaching process of manganese oxide ore to produce manganese sulfate using sulfur dioxide is widely used due to its clean and environmentally friendly nature, short production process, and low cost. However, in practical applications, continuous improvement of equipment to ensure efficient absorption of sulfur dioxide gas, thereby guaranteeing high manganese leaching and low sulfur oxide emissions in the tail gas, is a hot research topic. Chinese patent CN108193047B mentions a device for treating sulfur dioxide-containing flue gas from manganese ore slurry. This device can achieve a manganese leaching rate of over 94.3% while reducing the high concentration of sulfur dioxide in the flue gas to 100 mg / m³. 3 However, the following methods are not feasible. They require a large number of spray absorption towers, resulting in high investment costs and complex internal structures. Furthermore, the screen plates are prone to scaling and clogging during long-term operation with high-solids-content slurries. Chinese Patent CN110102170B discloses a desulfurization absorption tower that uses a multi-layer spray network with spray heads and employs a micro-cyclone separator to replace the traditional demister. This tower offers advantages such as high desulfurization efficiency and fast separation speed. However, when applied to slurry systems with high-concentration salt solutions and high-solids-content slurries, it still suffers from drawbacks such as an excessive number of spray heads, frequent clogging of the spray head orifices, and difficulty in maintenance and cleaning. Therefore, this invention aims to develop an absorption reaction device with a simple structure, low manufacturing cost, easy operation and maintenance, high sulfur dioxide absorption efficiency, and low tail gas emissions to better meet the actual production needs of sulfur dioxide reduction leaching of manganese ore. Utility Model Content

[0003] The technical problem solved by this utility model is to provide an absorption reaction device for reducing and leaching manganese ore with sulfur dioxide, so as to overcome the shortcomings in the above-mentioned background technology.

[0004] The technical problem solved by this utility model is achieved by the following technical solution:

[0005] An absorption reaction device for sulfur dioxide reduction leaching of manganese ore.

[0006] Includes absorption tower and circulation tank;

[0007] The absorption tower includes a tower body, a waste discharge pipe at the top of the tower body, and a first liquid discharge pipe at the bottom or lower part of the tower body. A first reactor, a second reactor, and a third reactor are arranged sequentially from top to bottom inside the tower body. The first reactor is connected to a feed pipe for supplying fresh slurry to the first reactor. The second and third reactors are respectively connected to the circulation tank via slurry return pipes. Each of the first, second, and third reactors has a discharge port at its bottom, through which the reacted slurry is sprayed downwards. The first and second reactors are provided with vent holes.

[0008] The circulation tank is connected to the absorption tower through the first drain pipe. The circulation tank is also equipped with an inlet pipe, an outlet pipe, and a second drain pipe. The inlet pipe is used to supply sulfur dioxide raw gas into the circulation tank, and the outlet pipe passes through the tower body and is connected to the inlet of the third reactor.

[0009] In this invention, the first reactor, the second reactor, and the third reactor each include an upper air inlet chamber and a lower reaction chamber. The air inlet chamber and the reaction chamber are internally connected. The bottom of the air inlet chamber has a converging conical structure, and the bottom of the reaction chamber has an outwardly expanding trumpet-shaped structure. The feed pipe extends to the bottom of the air inlet chamber of the first reactor and has a gap with the air inlet chamber. The two slurry return pipes extend to the bottom of the air inlet chambers of the second reactor and the third reactor, respectively, and have gaps with the air inlet chambers. The ends of the feed pipe and the two slurry return pipes are all provided with conical nozzles.

[0010] In this invention, the ratio of the cross-sectional area of ​​the end of the conical nozzle to the cross-sectional area of ​​the feed pipe or slurry return pipe is 1:5 to 10.

[0011] In this invention, the inner diameter of the end of the conical nozzle is not less than 12mm.

[0012] In this invention, the air holes are disposed on the air inlet chambers of the first reaction chamber and the second reactor, and the air holes are distributed in a matrix on the air inlet chamber.

[0013] In this invention, the ratio of the sum of the areas of the air holes on the first reactor to the cross-sectional area of ​​the feed pipe is 3 to 5:1; the ratio of the sum of the areas of the air holes on the second reactor to the cross-sectional area of ​​the corresponding slurry return pipe is 3 to 5:1.

[0014] In this invention, the diameter of the air pore is not less than 15mm.

[0015] In this invention, swirl components are provided at the bottom of the reaction chambers of the first reactor, the second reactor, and the third reactor.

[0016] In this invention, the swirl assembly includes multiple fan blades fixed to the inner wall of the reaction chamber. The multiple fan blades are evenly distributed around the center of the bottom of the reaction chamber, and the inclination angle between the fan blades and the horizontal plane is 30 to 60°.

[0017] In this invention, the bottom outer diameter of the reaction chambers of the first reactor, the second reactor, and the third reactor is at least 20 mm larger than the outer diameter of the air inlet.

[0018] Beneficial Effects: The sulfur dioxide reduction leaching manganese ore absorption reaction device of this utility model can achieve high-efficiency absorption reaction of sulfur dioxide flue gas in manganese ore leaching using a single tower and single tank structure. The equipment has low manufacturing and installation costs, is easy to operate and maintain, has high sulfur dioxide absorption efficiency, and low tail gas emissions. It solves the problem of existing technologies requiring more than two absorption towers with poor results. Using the absorption reaction device of this utility model, even if the sulfur dioxide volume content in the flue gas entering the circulation tank is as high as 10% to 13%, the sulfur dioxide in the tail gas discharged from the top of the tower is only 30 to 100 mg / m³. 3 The emissions are far below the national emission limits, therefore, this utility model has excellent practical promotion and application value. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of a preferred embodiment of the present invention.

[0020] Figure 2 This is a cross-sectional structural diagram of the first reactor or the second reactor in a preferred embodiment of the present invention.

[0021] Figure 3 This is a schematic diagram of the third reactor in a preferred embodiment of the present invention.

[0022] Figure 4 This is a top view of the third reactor in a preferred embodiment of the present invention.

[0023] Figure 5 This is a schematic diagram of the swirl assembly in a preferred embodiment of the present invention.

[0024] The components are as follows: 1. Absorption tower; 11. Tower body; 12. First reactor; 121. Inlet chamber; 122. Reaction chamber; 123. Swirl assembly; 124. Outlet; 125. Conical nozzle; 126. Vent; 13. Second reactor; 14. Third reactor; 15. Waste discharge pipe; 16. Feed pipe; 17. Slurry return pipe; 18. First drain pipe; 2. Circulation tank; 21. Inlet pipe; 22. Stirring mechanism; 23. Outlet pipe; 3. Second drain pipe; 4. Circulation pump; 5. Discharge pump. Detailed Implementation

[0025] To make the technical means, creative features, objectives and effects of this utility model easier to understand, the following description, in conjunction with specific illustrations, further elaborates on this utility model.

[0026] See Figures 1-5 As shown.

[0027] like Figure 1 As shown, the sulfur dioxide reduction leaching manganese ore absorption reaction device of this utility model includes an absorption tower 1 and a circulation tank 2. The absorption tower 1 includes a tower body 11, with a waste discharge pipe 15 installed at the top of the tower body 11. The tail gas after the sulfur dioxide gas is fully absorbed and reacted in the tower body 11 is discharged through the waste discharge pipe 15. A first drain pipe 18 is installed at the bottom or lower part of the tower body 11, and the slurry inside the tower body 11 enters the circulation tank 2 through the first drain pipe 18.

[0028] The tower body 11 is equipped with a first reactor 12, a second reactor 13, and a third reactor 14 arranged sequentially from top to bottom. The first reactor 12 is connected to a feed pipe 16, which can be connected to an external manganese slurry storage tank. The feed pipe 16 is used to supply fresh manganese slurry with a solid content of 10% to 35% into the first reactor 12. The second reactor 13 and the third reactor 14 are respectively connected to the circulation tank 2 through a slurry return pipe 17, which is connected to a circulation pump 4. This allows the manganese ore that has undergone reaction in the circulation tank 2 to be repeatedly absorbed and reacted in the second reactor 13 and the third reactor 14. The first reactor 12, the second reactor 13 and the third reactor 14 are all provided with discharge ports 124 at the bottom. The slurry after reaction is sprayed downward through the corresponding discharge port 124 and enters the circulation tank 2 through the first drain pipe 18 at the bottom of the tower body 11. The first reactor 12 and the second reactor 13 are all provided with vents 126. The sulfur dioxide gas remaining in the tower body 11 enters the second reactor 13 or the third reactor 14 through the vents 126 and reacts with the slurry.

[0029] In a preferred embodiment, the first reactor 12, the second reactor 13, and the third reactor 14 are arranged sequentially from top to bottom along the vertical axis of the tower body 11. In order to prolong the contact, absorption, and reaction time of the gas-liquid-solid three-phase material sprayed from the third reactor 14 during the falling process, the bottom of the third reactor 14 is at least 2m away from the bottom of the tower. In order to allow sufficient separation distance for the rising tail gas and prevent the tail gas from carrying vapor particles out of the tower, the top of the first reactor 12 is at least 2m away from the tail gas outlet at the top of the tower body 11.

[0030] like Figure 2 and Figure 3 and Figure 4As shown, the first reactor 12, the second reactor 13, and the third reactor 14 each include an upper air inlet chamber 121 and a lower reaction chamber 122. The air inlet chamber 121 and the reaction chamber 122 are internally connected. The bottom of the air inlet chamber 121 has a converging conical structure, and the bottom of the reaction chamber 122 has an outwardly expanding trumpet-shaped structure. The feed pipe 16 extends to the bottom of the air inlet chamber 121 of the first reactor 12 and has a gap with the air inlet chamber 121. The two slurry return pipes 17 extend to the bottom of the air inlet chambers 121 of the second reactor 13 and the third reactor 14, respectively, and have gaps with the air inlet chambers 121. The ends of the feed pipe 16 and the two slurry return pipes 17 are all provided with conical nozzles 125.

[0031] Fresh slurry enters the bottom of the air inlet chamber 121 of the first reactor 12 through the feed pipe 16 and is sprayed out into the reaction chamber 122 of the first reactor 12 through the conical nozzle 125 at the bottom. During the high-speed spraying of the slurry, the sulfur dioxide gas remaining in the tower body 11 enters the air inlet chamber 121 through the air hole 126 and is drawn into the reaction chamber 122 to fully react with the slurry. The reacted slurry is discharged in a rain curtain shape through the discharge port 124 at the bottom of the reaction chamber 122. The liquid material coming out of the circulation tank 2 enters the bottom of the air inlet chamber 121 of the second reactor 13 through the slurry return pipe 17 and is sprayed out into the reaction chamber 122 of the second reactor 13 through the conical nozzle 125 at the bottom. During the high-speed spraying of the slurry, the sulfur dioxide gas remaining in the tower body 11 enters the air inlet chamber 121 of the second reactor 13 through the air hole 126 and is drawn into the reaction chamber 122 to fully react with the slurry. The reacted slurry is discharged in a rain curtain shape through the discharge port 124 at the bottom of the reaction chamber 122.

[0032] In a preferred embodiment, in the first reactor 12, the ratio of the cross-sectional area of ​​the conical nozzle 125 at its tip to the cross-sectional area of ​​the feed pipe 16 is 1:5 to 10, preferably 1:8. In the second reactor 13 and the third reactor 14, the ratio of the cross-sectional area of ​​the conical nozzle 125 at its tip to the cross-sectional area of ​​the slurry return pipe is 1:5 to 10, preferably 1:8. The inner diameter of the tip of the conical nozzle 125 is not less than 12 mm, preferably 20 mm.

[0033] like Figure 5As shown, swirling components 123 are provided at the bottom of the reaction chambers 122 of the first reactor 12, the second reactor 13, and the third reactor 14. Each swirling component 123 includes multiple blades fixed to the inner wall of the reaction chamber 122. These blades are connected at the center of the bottom of the reaction chamber 122 and are evenly distributed circumferentially along the center of the bottom of the reaction chamber 122. The inclination angle of the blades to the horizontal plane is 30–60°, preferably 45°. This achieves the effect of forming a spiral spray of fine granular material when the gas-liquid-solid three-phase material is ejected at high speed from the reaction chambers 122 of the first reactor 12, the second reactor 13, and the third reactor 14 after the reaction is completed.

[0034] In a preferred embodiment, the bottom outer diameter of the reaction chamber 122 of the first reactor 12, the second reactor 13, and the third reactor 14 is at least 20 mm larger than the outer diameter of the air inlet chamber 121, thereby facilitating the achievement of a rain curtain effect. In a further preferred embodiment, the bottom outer diameter of the reaction chamber 122 of the third reactor 14 is 30 mm larger than the outer diameter of the air inlet chamber 121, while the bottom outer diameter of the reaction chamber 122 of the first reactor 12 and the second reactor 13 is 20 mm larger than the outer diameter of the air inlet chamber 121. This allows the slurry sprayed from the first reactor 12 and the second reactor 13, located at a higher position, to drip down onto the outer shell of the third reactor 14 located below, forming a multi-layered, interwoven rain curtain at the reaction chamber 122, further increasing the contact and reaction between the slurry and the gas inside the tower body 11.

[0035] The pores 126 are disposed on the air inlet chambers 121 of the first reaction chamber 122 and the second reactor 13. The pores 126 are matrix-distributed on the air inlet chambers 121. The ratio of the sum of the areas of the pores 126 on the first reactor 12 to the cross-sectional area of ​​the feed pipe 16 is 3 to 5:1, preferably 3:1. The ratio of the sum of the areas of the pores 126 on the second reactor 13 to the cross-sectional area of ​​the corresponding slurry return pipe 17 is 3 to 5:1, preferably 3:1. The pore diameter of the pores 126 is preferably 15 mm. This ensures that a sufficient amount of gas is introduced into the reactor to be fully absorbed and react with the slurry.

[0036] In this invention, the circulation tank 2 is also equipped with an inlet pipe 21, an outlet pipe 23, and a second drain pipe 3. The inlet pipe 21 is used to supply sulfur dioxide raw gas into the circulation tank 2. The outlet pipe 23 passes through the tower body 11 and is connected to the inlet of the third reactor 14. The sulfur dioxide raw gas undergoes an initial absorption reaction with the slurry in the circulation tank 2. The remaining sulfur dioxide gas enters the third reactor 14 to continue the reaction. The remaining sulfur dioxide gas after the reaction in the third reactor 14 diffuses to the tower body 11 and fully reacts with the rain curtain in the tower body 11 and with the adsorption in the first reactor 12 and the second reactor 13 in the reaction chamber 122. Therefore, after multiple absorption reactions, the residual sulfur dioxide in the tail gas discharged from the top of the tower body 11 is only 30-100 mg / m3.

[0037] The circulation tank 2 is equipped with a stirring assembly. In the circulation tank 2, the air inlet pipe 21 and the slurry return pipe 17 extend vertically downward from the top of the tank to the bottom of the tank. The depth of the extension is 0.4 meters from the bottom of the tank. During operation, the slurry level in the tank is controlled to be between 1.0 and 1.5 meters above the pipe opening.

[0038] This invention uses submerged gas absorption of sulfur dioxide flue gas in the circulation tank 2 as the first absorption reaction, combined with a stirring component to quickly achieve a mixing and diffusion effect, further promoting the absorption reaction efficiency of sulfur dioxide and MnO2 in manganese ore slurry.

[0039] In this invention, the sulfur dioxide flue gas after the first absorption reaction in the circulation tank 2 is sent to the third reactor 14 through the outlet pipe 23. After a series of processes including spraying, sucking, mixing and absorption reaction with the slurry liquid sent by the circulation pump 4, the flue gas is sprayed down in the tower in the form of a spiral spray flow, and then the residual gaseous sulfur dioxide in the tower is washed and absorbed again.

[0040] In this invention, the outer walls of the inlet chambers 121 of the second reactor 13 and the first reactor 12 are made of mesh as air intakes to absorb the rising gas phase flow in the tower. The material sprayed from the reactor at the higher position drips down to the outer shell of the reactor at the lower position and forms a rain curtain effect, which effectively washes the gas phase flowing out of the reaction chamber 122.

[0041] This invention has a simple structure and uses high-flow-rate slurry injection, which is not prone to scaling and clogging. It is particularly suitable for slurry reaction systems with high solids content. It does not require complex packing absorption layers, baffle layers, gas distribution and liquid distribution layers, thus avoiding slurry clogging in the packing layers and other tower layers.

[0042] This invention achieves high-efficiency absorption of high-concentration sulfur dioxide flue gas using only a single-tank, single-tower device, overcoming the drawbacks of existing multi-tower designs requiring two or more absorption towers. When the sulfur dioxide volume content of the raw flue gas is as high as 0.5% to 15%, the sulfur dioxide content of the discharged tail gas is only 30 to 100 mg / m³. 3 It is far below the emission limits set by the state.

[0043] In the description of this utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc., indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the accompanying drawings, and are only for the convenience of describing this utility model and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model.

[0044] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this utility model, "multiple" means two or more, unless otherwise explicitly specified.

[0045] In this utility model, unless otherwise explicitly specified and limited, the terms "installation", "connection", "linking", "fixing", etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components.

[0046] The above description, in conjunction with specific embodiments, provides a further detailed explanation of the present invention. It should not be construed that the specific implementation of the present invention is limited to these descriptions. For those skilled in the art, several simple deductions or substitutions can be made without departing from the concept of the present invention.

Claims

1. An absorption reaction device for sulfur dioxide reduction leaching of manganese ore, characterized in that, Includes absorption tower and circulation tank; The absorption tower includes a tower body, a waste discharge pipe at the top of the tower body, and a first liquid discharge pipe at the bottom or lower part of the tower body. A first reactor, a second reactor, and a third reactor are arranged sequentially from top to bottom inside the tower body. The first reactor is connected to a feed pipe for supplying fresh slurry to the first reactor. The second and third reactors are respectively connected to the circulation tank via slurry return pipes. Each of the first, second, and third reactors has a discharge port at its bottom, through which the reacted slurry is sprayed downwards. The first and second reactors are provided with vent holes. The circulation tank is connected to the absorption tower through the first drain pipe. The circulation tank is also equipped with an inlet pipe, an outlet pipe, and a second drain pipe. The inlet pipe is used to supply sulfur dioxide raw gas into the circulation tank, and the outlet pipe passes through the tower body and is connected to the inlet of the third reactor.

2. The absorption reaction apparatus for sulfur dioxide reduction leaching of manganese ore according to claim 1, characterized in that, The first, second, and third reactors each include an upper air inlet chamber and a lower reaction chamber. The air inlet chamber and the reaction chamber are internally connected. The bottom of the air inlet chamber has a converging conical structure, and the bottom of the reaction chamber has an outward flared trumpet structure. The feed pipe extends to the bottom of the air inlet chamber of the first reactor and has a gap between it and the air inlet chamber. The two slurry return pipes extend to the bottom of the air inlet chambers of the second and third reactors respectively and have gaps between them. The ends of the feed pipe and the two slurry return pipes are all provided with conical nozzles.

3. The absorption reaction apparatus for sulfur dioxide reduction leaching of manganese ore according to claim 2, characterized in that, The ratio of the cross-sectional area of ​​the conical nozzle tip to the cross-sectional area of ​​the feed pipe or slurry return pipe is 1:5~10.

4. The absorption reaction apparatus for sulfur dioxide reduction leaching of manganese ore according to claim 2, characterized in that, The inner diameter of the end of the conical nozzle is not less than 12mm.

5. The absorption reaction apparatus for sulfur dioxide reduction leaching of manganese ore according to claim 2, characterized in that, The vents are disposed on the air inlet chambers of the first reactor and the second reactor, and the vents are distributed in a matrix on the air inlet chambers.

6. The absorption reaction apparatus for sulfur dioxide reduction leaching of manganese ore according to claim 5, characterized in that, The ratio of the sum of the areas of the pores on the first reactor to the cross-sectional area of ​​the feed pipe is 3~5:1; the ratio of the sum of the areas of the pores on the second reactor to the cross-sectional area of ​​the corresponding slurry return pipe is 3~5:

1.

7. The absorption reaction apparatus for sulfur dioxide reduction leaching of manganese ore according to claim 6, characterized in that, The diameter of the pores is not less than 15 mm.

8. The absorption reaction apparatus for reducing manganese ore with sulfur dioxide according to claim 2, characterized in that, Swirl components are installed at the bottom of the reaction chambers of the first reactor, the second reactor, and the third reactor.

9. The absorption reaction apparatus for sulfur dioxide reduction leaching of manganese ore according to claim 8, characterized in that, The swirl assembly includes multiple fan blades fixed to the inner wall of the reaction chamber. The multiple fan blades are evenly distributed around the center of the bottom of the reaction chamber, and the inclination angle between the fan blades and the horizontal plane is 30~60°.

10. The absorption reaction apparatus for sulfur dioxide reduction leaching of manganese ore according to claim 2, characterized in that, The bottom outer diameter of the reaction chambers of the first, second, and third reactors is at least 20 mm larger than the outer diameter of the air inlet.

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