Complete mixing type reactor for high-temperature flue gas denitration and wastewater treatment

Abstract

The utility model provides a full-mixing reactor for high-temperature flue gas denitration and wastewater treatment, which belongs to the technical field of pollutant treatment devices, and comprises a reaction tank body, a flue gas discharge cylinder communicated with the reaction tank body, an eave-shaped guide structure arranged at the bottom of the flue gas discharge cylinder, an up-flow cylinder arranged in the reaction tank body, the flue gas discharge cylinder arranged above the up-flow cylinder, and the flue gas discharge cylinder arranged above the up-flow cylinder. A catalyst collecting disc is arranged below the reaction tank body, a gas rising cap is arranged in the center of the catalyst collecting disc, the bottom of the gas rising cap is communicated with a high-temperature flue gas inlet pipe, a waste water inlet, a waste water outlet and a first ozonized air inlet are formed in the side wall of the reaction tank body, and a gas-liquid separator and a gas mixer are arranged in the flue gas discharging barrel; and a second ozonized air inlet is arranged between the two. High-temperature flue gas and waste water treatment are combined, waste water is heated through flue gas waste heat so as to improve the waste water treatment efficiency, meanwhile, flue gas denitration is conducted, and the temperature is lowered, so that follow-up treatment is facilitated.

Description

Technical Field

[0001] The utility model belongs to the technical field of pollutant treatment devices, and in particular relates to a fully mixed reactor used for high-temperature flue gas denitration and wastewater treatment. Background Art

[0002] At present, the high-temperature flue gas after the three wastes incineration treatment, after the heat is recovered by the waste heat boiler, the flue gas temperature is 300-500℃. In order to avoid low-temperature corrosion of sulfur and chlorine and the regeneration of dioxins, the flue gas at this temperature is usually quenched and cooled before desulfurization and denitrification treatment to achieve standard emissions. Therefore, the heat of the flue gas cannot be further fully utilized, and a large amount of quenching water is wasted for flue gas cooling.

[0003] At the same time, with increasingly stringent environmental protection requirements, wastewater treatment and discharge standards are constantly improving, and production companies are facing the arduous problem of upgrading standards. Since the concentration of wastewater pollutants at the end of the treatment process is low and most of them are difficult to degrade organic matter, the biochemical treatment method is not effective. Various advanced oxidation methods such as ozone catalytic oxidation, ultraviolet catalytic oxidation, and electrocatalytic oxidation are usually used to further remove pollutants in ordinary reactors. However, the low concentration of pollutants in the wastewater leads to low reaction efficiency and high treatment costs. Utility Model Content

[0004] The problem to be solved by the utility model is to provide a fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment, which combines high-temperature flue gas with wastewater treatment, utilizes flue gas waste heat to heat wastewater to improve wastewater treatment efficiency, and at the same time denitrifies the flue gas and reduces the temperature, which is beneficial to subsequent treatment.

[0005] In order to solve the above technical problems, the technical solution adopted by the utility model is: a fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment, including a reaction tank body and a flue gas exhaust tube, the top of the flue gas exhaust tube is a flue gas outlet, the bottom of the flue gas exhaust tube extends into the reaction tank body and is connected with the reaction tank body, the bottom of the flue gas exhaust tube is provided with an eaves-shaped guide structure, and the eaves-shaped guide structure is arranged around the bottom edge of the flue gas exhaust tube; an upflow tube that passes through from top to bottom is arranged in the reaction tank body, and the upflow tube is located below the flue gas exhaust tube and is coaxial with the flue gas exhaust tube It is arranged that the wall of the upflow cylinder is located below the eaves-like guide structure, and a top guide channel is arranged between the top of the upflow cylinder wall and the eaves-like guide structure; a catalyst collecting plate is arranged below the upflow cylinder, and a bottom guide channel is arranged between the catalyst collecting plate and the upflow cylinder, an air riser cap is arranged at the center of the catalyst collecting plate, and the bottom of the air riser cap is connected with the high-temperature flue gas inlet pipe, a wastewater inlet is arranged on the side wall of the reaction tank body, a wastewater outlet is arranged above the wastewater inlet, and a first ozonated air inlet is arranged below the wastewater inlet.

[0006] Furthermore, the first ozonated air inlet is communicated with an ozone aerator arranged around the inner wall of the reaction tank.

[0007] Furthermore, the wastewater outlet is communicated with an overflow trough arranged around the inner wall of the reaction tank.

[0008] Furthermore, a gas-liquid separator is arranged inside the smoke exhaust tube, and a gas mixer is arranged above the gas-liquid separator.

[0009] Furthermore, a second ozonated air inlet is provided between the gas mixer and the gas-liquid separator.

[0010] Furthermore, a manhole is provided on the side wall of the reaction tank body, and the manhole is located above the catalyst collecting plate. The manhole is used for inputting and taking out catalyst particles and for the maintenance of the utility model.

[0011] Furthermore, the eaves-shaped guide structure is arranged to be inclined downward from the inside to the outside.

[0012] Furthermore, the catalyst collecting plate is a bowl-shaped structure.

[0013] Due to the adoption of the above technical solution, the beneficial effects of the utility model are:

[0014] The utility model can realize the full mixing state of the substances in the reaction tank body through the cooperation of the air lifting cap, the rising flow tube and the eaves-shaped guide structure without using power equipment such as pumps, thereby saving energy.

[0015] The utility model does not need to consume additional cooling water, and directly introduces high-temperature flue gas and waste water through the bottom of the reaction tank body and the side of the reaction tank body, thereby realizing rapid cooling of the high-temperature flue gas.

[0016] The utility model reduces the temperature of high-temperature flue gas while evaporating and concentrating wastewater, thereby increasing the concentration of pollutants, increasing the reaction rate, and reducing the amount of wastewater discharged; the increase in wastewater temperature is also conducive to the oxidation and decomposition of pollutants.

[0017] The gas lifting cap of the utility model is installed at the central position of the bowl-shaped catalyst collecting plate, so that the catalyst particles separated by the gas-liquid separator can be settled on the catalyst collecting plate, and the high-temperature flue gas output by the gas lifting cap can re-fluidize the catalyst particles, so that the catalyst particles are in a fluidized state and evenly distributed in the entire reaction tank body, thereby increasing the reaction efficiency of organic pollutants and ozone.

[0018] In the utility model, a part of the ozonated air enters the interior of the reaction tank body from the first ozonated air inlet, and the ozone introduced into the reaction tank body is formed into tiny bubbles by the ozone aerator, which are fully contacted and mixed with the organic pollutants in the wastewater, so as to realize the open-loop chain breaking and oxidative decomposition of the organic pollutants; the other part enters the flue gas discharge tube from the second ozonated air inlet and is mixed with the flue gas after cooling through the gas mixer to realize ozone denitrification, which can not only increase the amount of ozone added in the wastewater treatment process to enhance the treatment effect, but also the residual ozone that enters the first ozonated air inlet and does not participate in the reaction can assist the denitrification reaction of the flue gas after cooling, so as to avoid waste. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] The present invention will be described in detail below with reference to the accompanying drawings and in combination with examples, and the advantages and implementation methods of the present invention will become more obvious. The contents shown in the accompanying drawings are only used to explain the present invention and do not constitute any limitation to the present invention. In the accompanying drawings:

[0020] Figure 1 It is a structural schematic diagram of the utility model.

[0021] In the figure:

[0022] 1. Gas mixer; 2. Gas-liquid separator; 3. Overflow tank; 4. Rising tube; 5. Catalyst particles; 6. Reactor body; 7. Catalyst collecting plate; 8. Rising cap; 9. Ozone aerator; 10. Manhole; 11. Smoke exhaust tube; 12. Eaves-shaped guide structure; 13. Wastewater inlet; 14. Wastewater outlet; 15. First ozonized air inlet; 16. Second ozonized air inlet; 17. Top guide channel; 18. Bottom guide channel. DETAILED DESCRIPTION

[0023] like Figure 1As shown, the utility model is a fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment, including a reaction tank body 6 and a flue gas exhaust tube 11, the top of the flue gas exhaust tube 11 is a flue gas outlet, the bottom of the flue gas exhaust tube 11 extends into the reaction tank body 6 and is connected with the reaction tank body 6, and an eaves-shaped guide structure 12 is arranged at the bottom of the flue gas exhaust tube 11, and the eaves-shaped guide structure 12 is arranged around the bottom edge of the flue gas exhaust tube 11, and the eaves-shaped guide structure 12 is arranged downwardly inclined from the inside to the outside; an upflow tube 4 that passes through from top to bottom is arranged in the reaction tank body 6, the upflow tube 4 is located below the flue gas exhaust tube 11, and is coaxially arranged with the flue gas exhaust tube 11, and the tube wall of the upflow tube 4 is located below the eaves-shaped guide structure 12 A top guide channel 17 is provided between the top of the upflow tube 4 and the eaves-shaped guide structure 12; a catalyst collecting plate 7 is provided below the upflow tube 4, and the catalyst collecting plate 7 is a bowl-shaped structure. A bottom guide channel 18 is provided between the catalyst collecting plate 7 and the upflow tube 4, and an air lift cap 8 is provided at the center of the catalyst collecting plate 7. The bottom of the air lift cap 8 is connected to the high-temperature flue gas inlet pipe, and an air outlet is provided below the brim of the air lift cap 8. A wastewater inlet 13 is provided on the side wall of the reaction tank body 6. The wastewater inlet 13 is located on one side of the upflow tube 4, a wastewater outlet 14 is provided above the wastewater inlet 13, and a first ozonated air inlet 15 is provided below the wastewater inlet 13.

[0024] The first ozonated air inlet 15 is communicated with an ozone aerator 9 (existing device) arranged around the inner wall of the reaction tank body 6 .

[0025] The wastewater outlet 14 is connected to the overflow trough 3 arranged around the inner wall of the reaction tank body 6. The position of the overflow trough 3 cannot be lower than the position of the top guide channel 17. In this embodiment, the overflow trough 3 and the top guide channel 17 are located at the same horizontal plane.

[0026] A gas-liquid separator 2 is arranged inside the smoke exhaust tube 11 , and a gas mixer 1 is arranged above the gas-liquid separator 2 .

[0027] A second ozonized air inlet 16 is provided between the gas mixer 1 and the gas-liquid separator 2 .

[0028] A manhole 10 is provided on the side wall of the reaction tank body 6, and the manhole 10 is located above the catalyst collecting plate 7. The manhole 10 is used for inputting and taking out the catalyst particles 5 and for the maintenance of the utility model.

[0029] Working process of this utility model:

[0030] Wastewater enters the space between the reaction tank body 6 and the upflow tube 4 from the wastewater inlet 13 and flows downward. At the same time, the high-temperature flue gas after incineration treatment enters the upflow tube 4 of the reaction tank body 6 through the upflow cap 8. At this time, the wastewater flows back outward from the top guide channel 17 formed by the top of the upflow tube 4 and the eaves-shaped guide structure 12, forming a circulating fully mixed state inside and outside the upflow tube 4 (due to the setting of the gas-liquid separator 2, wastewater cannot pass through, but flue gas can pass through).

[0031] In the above process, the high-temperature flue gas provides power for the full mixing of the wastewater and heats the wastewater to about 80°C, while the temperature of the high-temperature flue gas can be reduced to about 100°C.

[0032] The pollutants in the wastewater after treatment by upstream conventional biochemical equipment are mainly difficult to open the ring and break the chain of hard-to-degrade organic matter. The wastewater is heated by high-temperature flue gas to reduce its viscosity and is more conducive to increasing the reaction rate with ozone.

[0033] When the high-temperature flue gas enters the wastewater to achieve rapid cooling, the pollutants in the wastewater are concentrated as the water in the wastewater evaporates, which is beneficial to improving the reaction efficiency.

[0034] A portion of the ozonated air enters the interior of the reaction tank body 6 from the first ozonated air inlet 15, and the ozone introduced into the reaction tank body 6 is formed into tiny bubbles through the ozone aerator 9, which are fully contacted and mixed with the organic pollutants in the wastewater, thereby achieving the ring-opening, chain-breaking and oxidative decomposition of the organic pollutants. At the same time, catalyst particles 5 for ozone catalytic oxidation are put into the reaction tank body 6 to increase the reaction rate of ozone oxidation of organic pollutants. The catalyst particles 5 are in a fluidized state in the reaction tank body 6, and settle after being separated by the gas-liquid separator 2. After being collected by the catalyst collection plate 7 at the bottom of the reaction tank body 6, the catalyst particles 5 are re-fluidized by high-temperature flue gas, so that the catalyst particles 5 are evenly distributed throughout the reaction tank body 6, thereby increasing the reaction efficiency of organic pollutants and ozone.

[0035] The cooled flue gas passes through the gas-liquid separator 2 at the upper part of the reaction tank body 6 and enters the upper denitrification zone. Another part of the ozonated air generated by the ozone generator enters the flue gas exhaust pipe 11 from the second ozonated air inlet 16 and is mixed with the cooled flue gas through the gas mixer 1 to achieve ozone denitrification.

[0036] The gas-liquid separator 2 and the gas mixer 1 are both existing equipment, which realize the separation of gas and liquid and the mixing of gas. In this embodiment, the gas-liquid separator 2 can adopt a demister, and the gas mixer 1 can adopt a mixing grid.

[0037] The above embodiments of the present invention are described in detail, but the above contents are only preferred embodiments of the present invention and cannot be considered to limit the scope of implementation of the present invention. All equivalent changes and improvements made within the scope of the present invention should still fall within the scope of the present invention.

Claims

1. A fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment, characterized in that: The smoke exhaust tube comprises a reaction tank body and a smoke exhaust tube, the top of the smoke exhaust tube is a smoke outlet, the bottom of the smoke exhaust tube extends into the reaction tank body and is connected with the reaction tank body, an eaves-shaped guide structure is arranged at the bottom of the smoke exhaust tube, and the eaves-shaped guide structure is arranged around the bottom edge of the smoke exhaust tube; an upflow tube which passes through from top to bottom is arranged in the reaction tank body, the upflow tube is located below the smoke exhaust tube, and a top guide channel is arranged between the top of the tube wall of the upflow tube and the eaves-shaped guide structure; a catalyst collecting plate is arranged below the upflow tube, and a bottom guide channel is arranged between the catalyst collecting plate and the upflow tube, a riser cap is arranged at the center of the catalyst collecting plate, and the bottom of the riser cap is connected with a high-temperature smoke inlet pipe, a wastewater inlet is arranged on the side wall of the reaction tank body, a wastewater outlet is arranged above the wastewater inlet, and a first ozonated air inlet is arranged below the wastewater inlet.

2. The fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment according to claim 1, characterized in that: The first ozonated air inlet is communicated with an ozone aerator arranged around the inner wall of the reaction tank.

3. The fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment according to claim 1, characterized in that: The wastewater outlet is communicated with an overflow trough arranged around the inner wall of the reaction tank.

4. The fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment according to claim 1, characterized in that: A gas-liquid separator is arranged inside the smoke exhaust tube, and a gas mixer is arranged above the gas-liquid separator.

5. The fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment according to claim 4, characterized in that: A second ozonated air inlet is arranged between the gas mixer and the gas-liquid separator.

6. The fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment according to claim 1, characterized in that: The side wall of the reaction tank body is provided with a manhole, and the manhole is located above the catalyst collecting plate.

7. The fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment according to claim 1, characterized in that: The eaves-shaped guide structure is arranged to be inclined downward from the inside to the outside.

8. The fully mixed reactor for high-temperature flue gas denitrification and wastewater treatment according to claim 1, characterized in that: The catalyst collecting plate is in a bowl-shaped structure.

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