Adsorption removal system of high-temperature carbide particles in pitch smoke of waste liquid incinerator

Abstract

This utility model relates to the field of flue gas treatment technology, specifically to an adsorption and removal system for high-temperature carbonaceous particles from asphalt fumes in a waste liquid incinerator. It includes a waste liquid incinerator, which is sequentially connected to a waste heat boiler, an SCR denitrification reactor, an economizer, and an air preheater. The air preheater is connected to a bag filter via a flue. The bag filter has an ash hopper at its bottom, with an ash discharge pipe connected to the bottom of the ash hopper. A scraper conveyor connected to an ash bin is located below the ash discharge pipe. The bag filter is connected to a desulfurization tower via an induced draft fan, and an oxidation fan is connected to the desulfurization tower via a pipeline. An alumina powder adding mechanism is located above the flue. The system utilizes the strong adsorption capacity and loose microporous structure of alumina powder to effectively intercept asphalt fumes carbonaceous particles and volatile organic compounds in the flue gas. Furthermore, due to the alkaline oxide properties of alumina powder, it can neutralize the acidic components of the asphalt fumes, reducing corrosion to downstream equipment and pipelines and extending their service life.

Description

Technical Field

[0001] This utility model relates to the field of flue gas treatment technology, specifically to an adsorption and removal system for high-temperature carbonized particles in asphalt fumes from waste liquid incinerators. Background Technology

[0002] When incinerating asphalt slurry waste liquid, the organic components in the waste liquid volatilize and escape into the flue gas due to the high temperature, forming asphalt fumes. If the combustion temperature in the incinerator is too low (<800℃), the residence time of the flue gas in the furnace is too short, resulting in incomplete combustion of the asphalt fumes. These fumes then enter the desulfurization tower with the flue gas, affecting the quality of the ammonium sulfate slurry at the bottom of the desulfurization tower. If the combustion temperature in the incinerator is too high (>1000℃), the residence time of the flue gas in the furnace is too long, causing some of the asphalt fumes to carbonize into particles. These powdery asphalt fumes are often difficult to capture by bag filters and eventually penetrate the filter bags, entering the desulfurization tower along with the flue gas. Inside the desulfurization tower, a small amount of asphalt fumes are washed by the circulating liquid and enter the bottom of the tower, while most of the particles are discharged into the atmosphere from the top of the desulfurization tower along with the flue gas. This not only causes excessive particulate matter emissions in flue gas, resulting in environmental pollution, but also the asphalt fumes carbon particles falling to the bottom of the desulfurization tower affect the quality of the ammonium sulfate slurry. As a result, after the ammonium sulfate solution undergoes subsequent evaporation and crystallization, the finished ammonium sulfate product will have a small amount of black powder, affecting product sales.

[0003] Therefore, there is an urgent need to develop a technical solution that can effectively intercept asphalt fume carbide particles in order to achieve efficient adsorption of high-temperature carbide particles and improve the quality of ammonium sulfate slurry at the bottom of the desulfurization tower. Utility Model Content

[0004] This invention addresses the problem of the difficulty in capturing and adsorbing asphalt fume carbon particles by providing an adsorption and removal system for high-temperature carbon particles from asphalt fume incinerators.

[0005] To solve the above problems, the technical solution of this utility model is:

[0006] The present invention relates to an adsorption and removal system for high-temperature carbonaceous particles in asphalt fumes from a waste liquid incinerator. The system includes a waste liquid incinerator, which is sequentially connected to a waste heat boiler, an SCR denitrification reactor, an economizer, and an air preheater. The air preheater is connected to a bag filter via a horizontally arranged flue. The bag filter contains filter bags and has an ash hopper at its bottom. An ash discharge pipe is connected to the bottom of the ash discharge pipe, and a scraper conveyor connects to an ash bin below the ash discharge pipe. The clean air chamber inside the bag filter is connected to a desulfurization tower via an induced draft fan and a transport pipeline. An oxidation fan is connected to the transport pipeline via a pipeline. An alumina powder adding mechanism is located above the flue.

[0007] Furthermore, the alumina powder adding mechanism includes an alumina powder tank, the bottom of which is connected to a flue via a feeding pipe, and the feeding pipe is equipped with a valve.

[0008] The alumina powder canister is filled with alumina powder via a discharge chute and a bucket elevator connected to it.

[0009] Furthermore, the valves are a first star-shaped unloading valve and a first electric slide gate valve.

[0010] With the rotation of the star-shaped discharge valve, the alumina in the alumina powder tank enters the horizontal flue at the inlet of the bag filter through the discharge pipe and the electric slide valve.

[0011] Furthermore, a first air cannon is provided at the bottom of the alumina powder canister.

[0012] Control parameters are set using data from the CEMS online analyzer at the top of the desulfurization tower's exhaust chimney, and electrically connected to the first star-shaped discharge valve at the bottom of the alumina powder tank. Two first air cannons are installed on the conical surface at the bottom of the alumina powder tank. Through a PLC control system program, the high-pressure airflow from these cannons is used to prevent alumina powder from adhering to the inner wall of the tank, ensuring normal discharge from the first star-shaped discharge valve.

[0013] Furthermore, the connection end between the flue and the bag filter is provided with spiral guide vanes.

[0014] By installing spiral guide blades in the horizontal flue, alumina powder is uniformly mixed with the flue gas and eventually adheres to the surface of the bag filter bag in the baghouse dust collector, forming a pre-coating effect on the filter bag surface. This serves two purposes: firstly, it protects the filter bag from physical and chemical damage, forming an alkaline powder ash layer on the filter bag surface that isolates it from corrosive substances such as oil mist, water vapor, and sulfides in the flue gas, preventing the filter bag from directly contacting harmful components and preventing filter bag fiber blockage caused by water vapor condensation in low-temperature flue gas, thus reducing the risk of bag clogging; secondly, it can extend the service life of the filter bag. The pre-coated ash layer can reduce the mechanical wear of the filter bag by dust particles and mitigate chemical corrosion by neutralizing acidic gases such as SO2. Especially during the start-up and shutdown phases of the incinerator or when incinerating waste liquid containing asphalt slurry, the pre-coating can prevent unburned oil from adhering to the filter bag, reducing damage under abnormal operating conditions. To improve dust removal efficiency and stability, pre-coating enhances the surface properties of the filter media, accelerates dust layer formation, and enables the baghouse dust collector to quickly reach its designed filtration efficiency. This maintains stable pressure differential across the filter bags and prevents resistance fluctuations caused by dust penetration or excessive cleaning. Utilizing the strong adsorption capacity and loose microporous structure of the alumina powder on the pre-coated surface, it effectively intercepts asphalt fumes, carbonaceous particles, and volatile organic compounds in flue gas.

[0015] Furthermore, the dust filter bag is connected to a backflushing pipe.

[0016] After the PLC control system of the bag filter reaches the pressure difference set value (when the pressure difference between a certain group of inlet chambers and clean air chambers of the bag filter is greater than 2000Pa), it controls the compressed air to perform reverse pulse jet blowing on the filter bags through the back-blowing pipe, thereby realizing the self-cleaning of the filter bags. The particles attached to the surface of the filter bags are shaken off into the ash hopper at the bottom of the bag filter under the action of pulse air oscillation and impact.

[0017] Furthermore, the dust hopper at the bottom of the bag filter is equipped with a heat tracing coil and a second air cannon.

[0018] Furthermore, the ash discharge pipe is equipped with a second star-shaped unloading valve and a second electric slide gate valve.

[0019] The filtered particles collected in the ash hopper are kept under negative pressure by the exhaust fan at the bag filter outlet. This allows humid, cold air from the external environment to easily enter the ash hopper through the ash discharge pipe and come into contact with the particles accumulated on the inner wall of the ash hopper. Over time, this can easily cause the particles to clump together on the inner wall of the ash hopper, affecting subsequent ash removal. To prevent this clumping, steam tracing coils are installed on the outer wall of each ash hopper, and two secondary air cannons are installed on top of each ash hopper. Through a PLC control system program, the high-pressure airflow from these secondary air cannons is used to prevent particles from adhering to the inner wall of the ash hopper. The loosened dust is then discharged through a star-shaped discharge valve, and finally collected into the ash silo by a scraper conveyor.

[0020] Working principle:

[0021] The high-temperature flue gas from the waste liquid incinerator, driven by a downstream induced draft fan, sequentially passes through a waste heat boiler, an SCR denitrification reactor, a boiler economizer, and an incinerator air preheater. After this process, the flue gas temperature drops to approximately 160℃–180℃ before entering a baghouse dust collector to remove particulate matter. In the horizontal flue before the flue gas enters the baghouse dust collector, alumina powder is fed through a discharge chute to a bucket elevator, which then lifts it to an alumina powder tank. With the rotation of the first rotary valve, the alumina in the tank flows through a discharge pipe and a first electric slide gate valve into the horizontal flue at the baghouse dust collector inlet. By installing spiral guide blades within the horizontal flue, alumina powder is uniformly mixed with the flue gas and ultimately adheres to the surface of the bag filter bags in the baghouse dust collector, forming a pre-coating effect. Utilizing the strong adsorption capacity and loose microporous structure of the alumina powder on the pre-coated surface, it effectively intercepts asphalt fumes, carbonaceous particles, and volatile organic compounds in the flue gas. Control parameters are set using data from the CEMS online analyzer at the top of the desulfurization tower's exhaust chimney, electrically connected to the first star-shaped discharge valve at the bottom of the alumina powder tank. The rotation speed of the first star-shaped discharge valve can be dynamically adjusted based on the online analyzer data, maintaining a stable adsorption effect. Two first air cannons are installed on the conical surface at the bottom of the alumina powder tank. Through PLC control system programming, the high-pressure airflow from these cannons prevents alumina powder from adhering to the inner wall of the tank, ensuring normal discharge from the star-shaped discharge valve. Once the PLC control system of the bag filter reaches the set pressure difference (when the pressure difference between a certain group of inlet chambers and clean air chambers of the dust collector exceeds 2000Pa), it controls compressed air to perform reverse pulse jet cleaning of the filter bags through the back-blowing pipe, thereby achieving self-cleaning of the filter bags. Particles adhering to the surface of the filter bags are shaken off into the ash hopper at the bottom of the dust collector under the vibration and impact of the pulsed air. The steam heating coil on the outer wall of the ash hopper is kept open year-round to heat the hopper, preventing the particles accumulated on the inner wall from contacting the cold, humid air and thus preventing caking. Through the PLC control system program, the high-pressure airflow of the second air cannon is used to loosen the particles on the inner wall of the ash hopper, and the loosened particles are discharged through the second star-shaped discharge valve. The cleaned particles are then collected into the ash silo by a scraper conveyor. The filtered flue gas enters the clean gas chamber and is sent to the desulfurization tower through the outlet of the induced draft fan. Before entering the desulfurization tower, it is fully mixed with the oxidation fan. The temperature of the flue gas mixed with oxidation air drops to 120℃. After entering the desulfurization tower, the flue gas desulfurization is completed. The desulfurized flue gas is directly discharged into the atmosphere through the chimney at the top of the tower.

[0022] The beneficial effects of this utility model are as follows:

[0023] (1) The system described in this utility model utilizes the strong adsorption capacity of alumina powder and the loose microporous structure to effectively intercept asphalt smoke carbon particles and volatile organic compounds in flue gas. In addition, due to the alkaline oxide properties of alumina powder, it can neutralize the acidic components of asphalt smoke, reduce corrosion of downstream equipment and pipelines, and extend their service life.

[0024] (2) The system described in this utility model heats the ash hopper by keeping the steam heating coil on the outer wall open all year round, which can prevent the particles accumulated on the inner wall from coming into contact with the cold and humid air, thereby preventing caking. By setting the PLC control system program, the high-pressure airflow of the second air cannon is used to loosen the particles on the inner wall of the ash hopper, and the loosened particles are discharged through the second star-shaped discharge valve. Attached Figure Description

[0025] The accompanying drawings, which are included to provide a further understanding of the present invention, form part of this invention. In the drawings:

[0026] Figure 1 This is a schematic diagram of the adsorption and removal system for high-temperature carbonaceous particles in asphalt fumes from a waste liquid incinerator according to this utility model.

[0027] In the diagram: 1. Waste liquid incinerator; 2. Waste heat boiler; 3. SCR denitrification reactor; 4. Economizer; 5. Air preheater; 6. Flue; 601. Spiral guide vane; 7. Alumina powder tank; 701. First air cannon; 702. First star-shaped discharge valve; 703. First electric slide gate valve; 704. Discharge chute; 705. Bucket elevator; 8. Bag filter; 801. Filter bag; 802. Ash hopper; 803. Second air cannon; 804. Heating coil; 805. Second star-shaped discharge valve; 806. Second electric slide gate valve; 807. Ash drop pipe; 808. Clean air chamber; 809. Backflush pipe; 9. Exhaust fan; 901. Transport pipe; 10. Desulfurization tower; 11. Oxidation fan; 12. Scraper conveyor; 13. Ash silo. Detailed Implementation

[0028] The present invention will now be described in detail with reference to the embodiments.

[0029] Example 1

[0030] like Figure 1As shown, the adsorption and removal system for high-temperature carbonaceous particles in asphalt fumes from a waste liquid incinerator includes a waste liquid incinerator 1. The waste liquid incinerator 1 is sequentially connected to a waste heat boiler 2, an SCR denitrification reactor 3, an economizer 4, and an air preheater 5. The air preheater 5 is connected to a bag filter 8 via a horizontally arranged flue 6. The bag filter 8 is equipped with a filter bag 801 inside. The bottom of the bag filter 8 is equipped with an ash hopper 802. The bottom end of the ash hopper 802 is connected to an ash discharge pipe 807. Below the ash discharge pipe 807, a scraper conveyor 12 is connected to an ash silo 13. The clean air chamber 808 inside the bag filter 8 is connected to a desulfurization tower 10 via an induced draft fan 9 and a transport pipe 901. An oxidation fan 11 is connected to the transport pipe 901 via a pipe. An alumina powder adding mechanism is provided above the flue 6.

[0031] Understandably, the alumina powder adding mechanism includes an alumina powder tank 7, the bottom of which is connected to the flue 6 via a feeding pipe, and the feeding pipe is equipped with a valve.

[0032] The alumina powder tank 7 is filled with alumina powder through the unloading chute 704 and the bucket elevator 705 connected thereto.

[0033] It is understood that the valves are the first star-shaped discharge valve 702 and the first electric slide gate valve 703.

[0034] With the rotation of the star-shaped discharge valve, the alumina in the alumina powder tank 7 enters the horizontal flue 6 at the inlet of the bag filter 8 through the discharge pipe and the electric slide valve.

[0035] Understandably, the bottom of the alumina powder canister 7 is equipped with a first air cannon 701.

[0036] Control parameters are set based on data detected by the CEMS online analyzer at the top of the desulfurization tower's 10 exhaust chimneys, and electrically connected to the first star-shaped discharge valve 702 at the bottom of the alumina powder tank 7. Two first air cannons 701 are installed on the conical bottom surface of the alumina powder tank 7. Through PLC control system programming, the high-pressure airflow impact effect of the first air cannons 701 prevents alumina powder from adhering to the inner wall of the tank bottom, ensuring normal discharge from the first star-shaped discharge valve 702.

[0037] Understandably, the connection end between the flue 6 and the bag filter 8 is provided with spiral guide vanes 601.

[0038] By installing spiral guide vanes 601 inside the horizontal flue 6, alumina powder is uniformly mixed with flue gas inside the flue 6 and eventually adheres to the surface of the filter bag 801 of the bag filter 8, forming a pre-coating effect on the surface of the filter bag 801. This protects the filter bag 801 from physical and chemical damage. The alkaline powder ash layer formed on the surface of the filter bag 801 isolates the filter bag 801 from corrosive substances such as oil mist, water vapor, and sulfides in the flue gas, preventing the filter bag 801 from directly contacting harmful components and preventing fiber blockage of the filter bag 801 caused by water vapor condensation in the low-temperature flue gas, thus reducing the risk of bag clogging. In addition, it can extend the service life of the filter bag 801. The pre-coated ash layer can reduce the mechanical wear of the filter bag 801 by dust particles and reduce chemical corrosion by neutralizing acidic gases such as SO2. Especially during the start-up and shutdown of the incinerator or when incinerating waste liquid containing asphalt slurry, the pre-coating can prevent unburned oil from adhering to the filter bag 801 and reduce damage under abnormal operating conditions. To improve dust removal efficiency and stability, pre-coating enhances the surface properties of the filter media, accelerates dust layer formation, and enables the bag filter 8 to quickly reach its designed filtration efficiency. This maintains stable pressure differential in the filter bag 801, preventing resistance fluctuations caused by dust penetration or excessive cleaning. Utilizing the strong adsorption capacity and loose microporous structure of the alumina powder on the pre-coated surface, it effectively intercepts asphalt fumes, carbonaceous particles, and volatile organic compounds in the flue gas.

[0039] Understandably, the dust filter bag 801 is connected to the backflushing pipe 809.

[0040] After the PLC control system of the bag filter 8 reaches the pressure difference set value (when the pressure difference between a certain group of inlet chambers and clean air chambers 808 of the bag filter 8 is greater than 2000Pa), it controls the compressed air to perform reverse pulse jet blowing on the filter bag 801 through the back-blowing pipe 809, thereby realizing the self-cleaning of the filter bag. The particles attached to the surface of the filter bag are shaken off into the ash hopper 802 at the bottom of the bag filter 8 under the action of pulse air oscillation and impact.

[0041] Understandably, the dust hopper 802 at the bottom of the bag filter 8 is equipped with a heat tracing coil 804 and a second air cannon 803.

[0042] It is understandable that the ash discharge pipe 807 is equipped with a second star-shaped discharge valve 805 and a second electric slide gate valve 806.

[0043] The filtered particles collected in hopper 802 are kept under negative pressure by the exhaust fan 9 at the outlet of the bag filter 8. This allows cold, humid air from the external environment to easily enter hopper 802 through the ash discharge pipe 807 and come into contact with the particles accumulated on the inner wall of hopper 802. Over time, this can easily cause the particles to clump together on the inner wall of hopper 802, affecting subsequent ash removal. To prevent this clumping, a steam heating coil 804 is installed on the outer wall of each hopper 802, and two second air cannons 803 are installed on top of each hopper 802. Through a PLC control system program, the high-pressure airflow from the second air cannons 803 is used to prevent particles from adhering to the inner wall of hopper 802. The loosened dust is discharged through a star-shaped discharge valve and then collected by a scraper conveyor 12 into the ash silo 13.

[0044] Working principle:

[0045] The high-temperature flue gas from the waste liquid incinerator 1, under the action of the downstream induced draft fan 9, sequentially passes through the waste heat boiler 2, the SCR denitrification reactor 3, the boiler economizer 4, and the incinerator air preheater 5. After the flue gas temperature drops to about 160℃~180℃, it enters the bag filter 8 to remove particulate matter from the flue gas. In the horizontal flue 6 before the flue gas enters the bag filter 8, alumina powder is sent to the bucket elevator 705 through the unloading chute 704. The bucket elevator 705 then lifts it to the alumina powder tank 7. Under the rotation of the first star-shaped unloading valve 702, the alumina in the alumina powder tank 7 enters the horizontal flue 6 at the inlet of the bag filter 8 through the discharge pipe and the first electric slide valve 703. By installing spiral guide vanes 601 within the horizontal flue 6, alumina powder is uniformly mixed with the flue gas within the flue 6 and ultimately adheres to the surface of the filter bags 801 in the baghouse dust collector 8, forming a pre-coating effect on the filter bags 801. Utilizing the strong adsorption capacity and loose microporous structure of the alumina powder on the pre-coated surface, it effectively intercepts asphalt fumes, carbonaceous particles, and volatile organic compounds in the flue gas. Control parameters are set using data from the CEMS online analyzer at the top of the desulfurization tower 10's exhaust chimney. This is electrically connected to the first star-shaped discharge valve 702 at the bottom of the alumina powder tank 7. The rotation speed of the first star-shaped discharge valve 702 can be dynamically adjusted based on the data from the online analyzer, maintaining a stable adsorption effect. Two first air cannons 701 are installed on the conical bottom surface of the alumina powder tank 7. Through PLC control system programming, the high-pressure airflow impact effect of the first air cannons 701 prevents alumina powder from adhering to the inner wall of the tank bottom, ensuring normal discharge from the star-shaped discharge valve. After the PLC control system of the bag filter reaches the pressure difference set value (when the pressure difference between a certain group of inlet chambers and clean air chambers 808 of the dust collector is greater than 2000Pa), compressed air is controlled to perform reverse pulse jet blowing on the filter bags 801 through the back-blowing pipe 809, thereby achieving self-cleaning of the filter bags 801. Particles adhering to the surface of the filter bags 801 are shaken off into the ash hopper 802 at the bottom of the dust collector under the action of pulse air oscillation and impact. The steam heating coil 804 on the outer wall of the ash hopper 802 is kept open year-round to heat the ash hopper 802, preventing the particles accumulated on the inner wall from contacting the cold, humid air and thus preventing caking. Through the PLC control system program setting, the high-pressure airflow impact effect of the second air cannon 803 is used to loosen the particles on the inner wall of the ash hopper 802, and the loosened particles are discharged through the second star-shaped discharge valve 805. The cleaned particles are then collected into the ash silo 13 by the scraper conveyor 12. The filtered flue gas enters the clean gas chamber 808 and is sent to the desulfurization tower 10 through the outlet of the induced draft fan 9. Before entering the desulfurization tower 10, it is fully mixed with the oxidation fan 11. The temperature of the flue gas mixed with oxidation air drops to 120℃. After entering the desulfurization tower 10, the flue gas desulfurization is completed. The desulfurized flue gas is directly discharged into the atmosphere through the chimney at the top of the tower.

[0046] The above description is merely an embodiment of this utility model and is not intended to limit the scope of this utility model. Various modifications and variations can be made to this utility model by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principle of this utility model should be included within the scope of the claims of this utility model.

Claims

1. A system for adsorptive removal of high-temperature carbide particles of pitch fumes from a waste liquid incinerator, characterized in that The system includes a waste liquid incinerator (1), which is connected in sequence to a waste heat boiler (2), an SCR denitrification reactor (3), an economizer (4), and an air preheater (5). The air preheater (5) is connected to a bag filter (8) through a flue (6). The bag filter (8) is equipped with a filter bag (801) inside. The bottom of the bag filter (8) is equipped with an ash hopper (802). The bottom end of the ash hopper (802) is connected to an ash discharge pipe (807). Below the ash discharge pipe (807) is a scraper conveyor (12) connected to an ash silo (13). The clean air chamber (808) inside the bag filter (8) is connected to a desulfurization tower (10) through an induced draft fan (9) and a transport pipe (901). An oxidation fan (11) is connected to the transport pipe (901) through a pipe. An alumina powder adding mechanism is provided above the flue (6).

2. The system for removing high-temperature carbide particles of pitch smoke of waste liquid incinerator according to claim 1, characterized in that, The alumina powder adding mechanism includes an alumina powder tank (7), the bottom of which is connected to the flue (6) through a feeding pipe, and a valve is provided on the feeding pipe.

3. The system for removing high-temperature carbide particles of pitch smoke of waste liquid incinerator according to claim 2, characterized in that, The valves are a first star-shaped unloading valve (702) and a first electric slide gate valve (703).

4. The system for removing high-temperature carbide particles of pitch smoke of waste liquid incinerator according to claim 2, characterized in that, The bottom of the alumina powder canister (7) is equipped with a first air cannon (701).

5. The system for removing high-temperature carbide particles of pitch smoke of waste liquid incinerator according to claim 2, characterized in that, The flue (6) is connected to the bag filter (8) with a spiral guide vane (601) inside.

6. The system for removing high-temperature carbide particles of pitch smoke of waste liquid incinerator according to claim 1, characterized in that, The dust filter bag (801) is connected to the backflush pipe (809).

7. The system for removing high-temperature carbide particles of pitch smoke of waste liquid incinerator according to claim 1, characterized in that, The bottom hopper (802) of the bag filter (8) is equipped with a heat tracing coil (804) and a second air cannon (803).

8. The system for removing high-temperature carbide particles of pitch smoke of waste liquid incinerator according to claim 1, characterized in that, The ash discharge pipe (807) is equipped with a second star-shaped discharge valve (805) and a second electric slide gate valve (806).

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