CN107854924B - Activated coke dry method flue gas treatment method and system - Google Patents
Activated coke dry method flue gas treatment method and system Download PDFInfo
- Publication number
- CN107854924B CN107854924B CN201711264855.5A CN201711264855A CN107854924B CN 107854924 B CN107854924 B CN 107854924B CN 201711264855 A CN201711264855 A CN 201711264855A CN 107854924 B CN107854924 B CN 107854924B
- Authority
- CN
- China
- Prior art keywords
- active coke
- dust
- bubbling
- flue gas
- coke particles
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/30—Particle separators, e.g. dust precipitators, using loose filtering material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/66—Regeneration of the filtering material or filter elements inside the filter
- B01D46/70—Regeneration of the filtering material or filter elements inside the filter by acting counter-currently on the filtering surface, e.g. by flushing on the non-cake side of the filter
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses an active coke dry method flue gas treatment method and a system, wherein the treatment method comprises the following steps: s10: the purification tower removes dust from the dust-containing flue gas; s20: the method comprises the following steps that dust-containing active coke particles and active coke particles in a purification tower enter a first bubbling area, dust in the dust-containing active coke particles and the active coke particles are separated in the first bubbling area, the dust enters dust removal equipment, and the active coke particles enter a regeneration tower; s30: regenerating the activated coke particles; s40: screening the regenerated active coke, conveying the regenerated active coke with small particle size into an ash tank, and conveying the regenerated active coke with large particle size into a second bubbling region; s50: in the second bubbling area, the dust and the regenerated active coke particles are separated, the dust is conveyed to a dedusting device, the regenerated active coke particles enter a purification tower, and the step S10 is executed again. In the technical field of purification by an active coke-drying method, the treatment method disclosed by the invention is easy to operate, high in dust removal efficiency, low in operation cost and capable of effectively reducing the dust content of the discharged gas.
Description
Technical Field
The invention relates to the technical field of flue gas treatment, in particular to an active coke dry method flue gas treatment method and system.
Background
The key industries related to dust removal in China mainly comprise the industries of thermal power, steel, cement, nonferrous metal, petrochemical industry, chemical industry, waste incineration and the like. In a plurality of flue gas combined desulfurization and denitrification technologies, the active coke dry method can simultaneously remove SO in flue gas 2 And NO x The pollutants can also remove heavy metals such as dust, mercury and the like and volatile organic compounds in the flue gas, and the emission concentrations of the smoke dust, sulfur dioxide and nitrogen oxides are respectively not higher than 5, 35 and 50mg/m under the condition that the ultralow emission requirement of the coal-fired thermal power plant is 6 percent of the reference oxygen content 3 New requirements are put forward on the prior art. The active coke dry purification technology adopts sulfur dioxide and nitrogen oxide to realize new environmental protection requirements through process design parameter adjustment and reactor optimization, and the active coke moving bedAs a particle dust remover, the improvement of dust removal efficiency through optimization of the reactor is limited, and new environmental requirements cannot be met.
The ultra-low dust emission of the existing flue gas treatment system is generally realized by adding a wet-type electric dust collector, the electric dust collector can be upgraded and modified into a low-temperature electric dust collector or an electric bag composite dust collector, an electric coagulation technology, a high-frequency power supply technology, a rotary electrode type electric dust collection technology and the like can be adopted to improve the electric dust collection efficiency, and the investment cost and the running cost are increased. The active coke dry purification technology adopts a moving bed, the moving bed is used as a granular layer filter, one part of smoke dust is intercepted, the smoke dust continuously moves downwards under the action of gravity, the smoke dust leaves at the lower end of a purification device, the active coke and the active coke are rubbed in the moving process to generate active coke powder, the purification technology does not need to additionally increase dust removal equipment such as wet-type electric dust removal equipment, however, the active coke powder generated in the material conveying process by the active coke dry purification technology is used, the dust content in the outlet gas of a purification tower and the regeneration gas of the regeneration tower is increased, the dust content in the purified smoke gas does not reach the ultralow emission index, the dust content in the regeneration gas is higher, and the purification technology is not beneficial to the conveying of the regeneration gas and a subsequent byproduct treatment system.
Therefore, there is a need for a method and a system for active coke dry flue gas treatment, which has low operation cost and low dust content in the exhaust gas.
Disclosure of Invention
The invention aims to provide an active coke dry method flue gas treatment method and system, in the technical field of active coke dry method purification, the treatment method is easy to operate, has high dust removal efficiency, can effectively remove dust from active coke particles, and can also effectively reduce the dust content in the exhaust gas.
The technical scheme provided by the invention is as follows:
an active coke dry method flue gas treatment method comprises the following steps:
s10: the method comprises the following steps that (1) dust-containing flue gas enters a purification tower provided with an active coke particle layer, and the purification tower carries out dust removal treatment on the dust-containing flue gas;
s20: when the regeneration tower normally operates, active coke particles generated by mutual collision and friction between dust-containing active coke particles and active coke particle layers in the purification tower are conveyed to a first bubbling area, dust and active coke particles in the dust-containing active coke particles are separated in the first bubbling area, the separated dust is conveyed to a dust removal device, the active coke particles obtained after separation enter the regeneration tower, and in the step, a bubbling medium is continuously conveyed to the first bubbling area;
s30: the regeneration tower regenerates the active coke particles passing through the first bubbling zone to obtain regenerated active coke;
s40: screening the regenerated active coke, conveying the regenerated active coke with the particle size smaller than a preset particle size to an ash tank for storage, conveying the regenerated active coke with the particle size larger than the preset particle size to a second bubbling area, and continuously conveying a bubbling medium to the second bubbling area in the step;
s50: and in the second bubbling area, separating the dust in the regenerated active coke with the particle size larger than the preset particle size from the regenerated active coke particles, conveying the separated dust to the dust removal equipment, feeding the separated regenerated active coke particles into the purification tower, and executing the step S10 again.
Preferably, the active coke-drying flue gas treatment method further comprises step S60: introducing the flue gas obtained after dust removal in the dust removal equipment into the purification tower; and/or; in the step S20, the dust generated in the process that the activated coke particles and dust-containing activated coke particles in the purification tower are conveyed to the first bubbling zone is conveyed to the dust removing equipment; and/or; in the step S40, the dust generated in the process of conveying the regenerated activated coke with the particle size larger than the preset particle size to the second bubbling zone is conveyed to the dust removing equipment.
Preferably, in the step S20, the first bubbling zone is arranged in a first vertical pipeline, the active coke particles and dust-containing active coke particles in the purification tower are conveyed to the first bubbling zone through a first chute, and an included angle between the first chute and the first vertical pipeline is an acute angle; and/or; in the step S40, the second bubbling region is disposed in a second vertical pipe, the regenerated active coke with a particle size larger than a preset particle size is conveyed to the second bubbling region through a second chute, and an included angle between the second chute and the second vertical pipe is an acute angle.
Preferably, in the step S20, the flow speed of the bubbling medium is 0.8-1.5 m/S; in step S40, the flow rate of the bubbling medium is 0.8 to 1.5m/S.
Preferably, after the step S10, the method further comprises the steps of:
s70: when the regeneration tower breaks down, the active coke particles and the dust-containing active coke particles in the purification tower are conveyed to a third bubbling area, dust and active coke particles in the dust-containing active coke particles are separated in the third bubbling area, the separated dust is conveyed to a dust removal device, the active coke particles obtained after separation enter a storage bin, and in the step, a bubbling medium is continuously conveyed to the third bubbling area;
s80: and (2) conveying the active coke particles in the storage bin to the second bubbling area, performing secondary dust removal treatment on the active coke particles output by the storage bin in the second bubbling area, conveying the treated dust to the dust removal equipment, conveying the treated active coke particles to the purification tower, and executing the step S10 again.
Preferably, the active coke dry method flue gas treatment method of the invention further comprises a step S90: supplemental activated coke is delivered to the third bubbling zone.
The invention also discloses an active coke dry-method flue gas treatment system, which comprises a purification tower for purifying flue gas and a regeneration tower for regenerating active coke, wherein an active coke moving bed is arranged in the purification tower, the purification tower conveys active coke particles containing dust and the active coke particles generated by mutual collision and friction between the active coke particles and the regeneration tower through a first conveyor, and a first bubbling area is arranged between the outlet of the first conveyor and the inlet of the regeneration tower; the pipeline positioned at the upstream of the first bubbling region is communicated with dust removing equipment, the pipeline positioned at the downstream of the first bubbling region is communicated with a fan, and the fan is used for conveying a bubbling medium to the first bubbling region; the regeneration tower conveys the regenerated active coke particles to the purification tower through a second conveyor; a screening device is arranged between the inlet of the second conveyor and the outlet of the regeneration tower, a first outlet of the screening device is communicated with the second conveyor, and a second outlet of the screening device is communicated with the ash tank; a second bubbling area is arranged between the outlet of the second conveyor and the inlet of the purification tower; and the pipeline positioned at the upstream of the second bubbling region is communicated with the dust removing equipment, and the pipeline positioned at the downstream of the second bubbling region is communicated with a fan which is used for conveying a bubbling medium to the second bubbling region.
Preferably, the flue gas outlet of the dust removal equipment is communicated with the flue gas inlet of the purification tower; and/or; the first conveyor is communicated with the dust removal equipment through a first dust removal pipeline; and/or; the second conveyor is communicated with the dust removal equipment through a second dust removal pipeline.
Preferably, the first bubbling region is arranged in a first vertical pipeline, the outlet of the first conveyor is communicated with the first vertical pipeline through a first chute, and the included angle between the first chute and the first vertical pipeline is an acute angle; and/or; the second bubbling area is arranged in a second vertical pipeline, an outlet of the second conveyor is communicated with the second vertical pipeline through a second chute, and an included angle between the second chute and the second vertical pipeline is an acute angle.
Preferably, the flow speed of the bubbling medium conveyed to the first bubbling zone and the second bubbling zone by the fan is 0.8-1.5 m/s.
Preferably, the active coke-drying flue gas treatment system further comprises: the material storage bin is characterized in that a feeding port of the material storage bin is communicated with a discharge port of the first conveyor, a third bubbling area is arranged between the feeding port of the material storage bin and the discharge port of the first conveyor, a valve is arranged on a communication pipeline between the first conveyor and the third bubbling area, a pipeline positioned on the upstream of the third bubbling area is communicated with the dust removal equipment, and a pipeline positioned on the downstream of the third bubbling area is communicated with the fan.
Preferably, the active coke-drying flue gas treatment system further comprises: and the charging hopper conveys supplementary active coke to the storage bin through a third conveyor, and a discharge hole of the third conveyor is communicated with a feed inlet of the storage bin through a third bubbling area.
Preferably, the discharge port of the first conveyor is communicated with the storage bin through the third bubbling region, and a valve is arranged on a communication pipeline between the first conveyor and the third bubbling region.
The active coke dry method flue gas treatment method and the system provided by the invention can bring at least one of the following beneficial effects:
1. the active coke dry-method flue gas treatment method provided by the invention has the advantages that when the active coke particles and the dust-containing active coke particles are conveyed into the regeneration tower by the purification tower, the first bubbling area is used for carrying out first dust removal on the active coke particles, the active coke after dust removal enters the regeneration tower for regeneration, the regenerated active coke is used for removing the particles with smaller particle sizes through the screening device, the particles with larger residual particle sizes are input into the purification tower for recycling after secondary dust removal, the steps of the method are simple and easy to operate, the dust in the active coke particles can be effectively removed through multiple bubbling and purging, the active coke particles can be recycled, the dust in the exhaust gas is effectively reduced, the dust removal efficiency is improved, the conveying of the regeneration gas and the treatment of subsequent byproducts are facilitated, and the investment cost and the operation cost are low.
2. In the invention, the flue gas after dust removal is introduced into the purification tower again, so that the gas can be subjected to multiple circulating dust removal, thereby further reducing the dust content in the discharged gas.
3. According to the invention, the dust generated when the conveyor conveys the active coke particles is conveyed to the dust removal equipment, so that the treatment capacity of a bubbling area can be reduced, the energy consumption required by bubbling is reduced, and the dust removal efficiency is further improved.
4. According to the active coke particle removing device, the conveyor conveys active coke particles to the bubbling region through the chute inclined to the pipeline of the bubbling region, and when the active coke particles are arranged in this way, a certain included angle is formed between the direction of the active coke particles entering the bubbling region and the flowing direction of a bubbling medium, so that the bubbling medium can effectively remove dust attached to the active coke particles in the bubbling process.
5. According to the invention, when the regeneration tower breaks down, the storage bin is arranged, so that the dust-containing active coke in the purification tower can return to the purification tower for recycling after bubbling and dedusting twice, an operator can repair the regeneration tower in time conveniently, and the treatment efficiency of the whole system can be effectively ensured by conveying the supplementary active coke to the storage bin.
6. The flue gas treatment system adopting the active coke drying method has a simple structure, is easy to install, and can effectively remove dust in active coke particles and reduce dust in discharged flue gas.
7. The active coke dry method flue gas treatment system can be directly improved on the existing dry method flue gas treatment system, and has the advantages of small change to the original system and low investment and operation cost.
8. The active coke-drying flue gas treatment system effectively reduces the dust content in the regenerated gas, and is beneficial to conveying the regenerated gas and simplifying the treatment of subsequent byproducts.
Drawings
The above features, technical features, advantages and modes of realisation of the present invention will be further described in the following detailed description of preferred embodiments thereof, which is to be read in connection with the accompanying drawings.
FIG. 1 is a schematic structural diagram of one embodiment of an active coke dry flue gas treatment system of the present invention;
FIG. 2 is a schematic diagram of another embodiment of the active coke dry flue gas treatment system of the present invention.
The reference numbers illustrate:
1. dust-containing flue gas; 2. a first feed discharger; 3. a bin is arranged at the top; 4. a purification tower; 5. purifying the flue gas; 6. a first discharge unloader; 7. a first conveyor; 7-1, a first dust removal pipeline; 8. a second feed discharger; 9. a regeneration tower; 10. a second discharge unloader; 11. vibrating the screen; 12. a second conveyor; 12-1, a second dust removal pipeline; 13. a first ash discharge valve; 14. a gate valve; 15. a storage bin; 16. a third discharge unloader; 17. a third conveyor; 18. fresh activated coke; 19. a hopper; 20. a dust removal device; 21. a second ash discharge valve; 22. an ash tank; 23. a dust removal fan; 24. bubbling medium air; 25. A fan; 26. a second sparge gas line; 26-1, a second bubbling zone; 26-2, a second chute; 26-3, a second dusty gas pipeline; 27. a first sparge gas line; 27-1, a first sparging zone; 27-2, a first chute; 27-3, a first dirty gas line; 28. a third bubbling gas line; 28-1, a third bubbling zone; 28-2, a third chute; 28-3 and a third dust-containing gas pipeline.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following description will be made with reference to the accompanying drawings. It is obvious that the drawings in the following description are only some examples of the invention, and that for a person skilled in the art, without inventive effort, other drawings and embodiments can be derived from them. For the sake of simplicity, the drawings only schematically show the parts relevant to the present invention, and they do not represent the actual structure as a product.
Detailed description of the preferred embodiment
An active coke dry method flue gas treatment method comprises the following steps:
s10: the dust-containing flue gas enters a purification tower provided with an active coke particle layer, and the purification tower carries out dust removal treatment on the dust-containing flue gas;
s20: when the regeneration tower normally operates, active coke particles generated by mutual collision and friction between dust-containing active coke particles in the purification tower and active coke particle layers are conveyed to a first bubbling area, dust generated in the conveying process is conveyed to dust removal equipment, the dust in the dust-containing active coke particles is separated from the active coke particles in the first bubbling area, the separated dust is conveyed to the dust removal equipment, the separated active coke particles enter the regeneration tower, and in the step, a bubbling medium is continuously conveyed to the first bubbling area;
s30: the regeneration tower regenerates the active coke particles passing through the first bubbling zone to obtain regenerated active coke;
s40: screening the regenerated active coke, conveying the regenerated active coke with the particle size smaller than the preset particle size to an ash tank for storage, conveying the regenerated active coke with the particle size larger than the preset particle size to a second bubbling area, conveying dust generated in the process of conveying the regenerated active coke with the particle size larger than the preset particle size to a dust removal device, and continuously conveying a bubbling medium to the second bubbling area in the step;
s50: and in the second bubbling area, separating the dust in the regenerated active coke with the particle size larger than the preset particle size from the regenerated active coke particles, conveying the separated dust to the dust removal equipment, feeding the separated regenerated active coke particles into the purification tower, and executing the step S10 again.
Specifically, the active coke-drying flue gas treatment method further comprises the step S60: and introducing the flue gas obtained after dust removal in the dust removal equipment into the purification tower. Through the steps, the flue gas can be purified and dedusted for multiple times, so that the dust and pollutants in the discharged flue gas are further reduced.
Specifically, in step S20, a first bubbling region is disposed in the first vertical pipe, the active coke particles and the dust-containing active coke particles in the purification tower are conveyed to the first bubbling region through a first chute, and an included angle between the first chute and the first vertical pipe is an acute angle. In addition, in step S40, a second bubbling region is disposed in the second vertical pipe, and the regenerated active coke with the particle size larger than the preset particle size is conveyed to the second bubbling region through a second chute, wherein an included angle between the second chute and the second vertical pipe is an acute angle. Specifically, the size range of the first slide pipe and the second slide pipe is 150-400 mm, the cross section of the first slide pipe and the second slide pipe is square or circular, and the included angle between the slide pipes and the vertical pipeline is 30-55 degrees.
Specifically, the flow rate of the bubbling medium is 0.8 to 1.5m/S in step S20, and the flow rate of the bubbling medium is 0.8 to 1.5m/S in step S40.
The particle sizes of the active coke particles and the dust particles are different, and different particles have specific critical bubbling velocity (umf) and terminal velocity (ut) according to the fluidization theory. When the average gas velocity (um) passing through the bed layer is greater than the critical bubbling velocity of the particles, the active coke particles can enter a bubbling state, and when the average gas velocity is greater than the terminal velocity, the particles are carried out along with the gas. By utilizing the characteristics, active coke particles containing dust are introduced into the bubbling bed, the flow speed of an operation bubbling medium is controlled to be higher than the critical bubbling speed of the active coke particles and the terminal speed of the dust, the bed layer is in a bubbling state under the terminal speed of the active coke particles, and gas is fully contacted with the active coke particles, so that the dust attached to the active coke particles is separated from the active coke particles and is carried out along with the gas, and the separation of the active coke and the dust is realized.
Critical bubbling velocity u of particles mf As shown in formula 1:
terminal velocity u of the particle t As shown in formula 2:
in the above formula:
Φ s -a particle shape factor; ε mf-critical void fraction; d p -the particle diameter, m;
ρ g gas phase density, kg/m 3 ；ρ s Particle density, kg/m 3 (ii) a μ -gas phase viscosity, pa.s.
In specific implementation, the flow rate of the bubbling medium can be specifically set according to the above formula according to actual needs.
In the active coke dry-method flue gas treatment method in the specific embodiment, dust in active coke particles is effectively removed through multiple times of multi-point bubbling for dust removal, so that the active coke particles with larger particles can be recycled, and in addition, the flue gas treated by the method has low dust content and small pollution to the environment.
Certainly, in other specific embodiments of the active coke dry method flue gas treatment method of the invention, the flue gas after dust removal in the dust removal equipment can also be directly discharged without being conveyed into the purification tower; dust generated in the process of conveying the active coke by the conveyor can directly enter the bubbling area along with the active coke particles; in addition, the conveyer can also be through horizontal conveying pipe with active burnt granule transport bubbling district, the active burnt granule enters into the contained angle between the direction in bubbling district and the flow direction of bubbling medium and can adjust according to actual need, and it is no longer repeated here.
Detailed description of the invention
The specific embodiment discloses another specific embodiment of the active coke dry method flue gas treatment method, and compared with the first specific embodiment, the specific embodiment further comprises the following steps after the step S10:
s70: when the regeneration tower breaks down, the active coke particles and the dust-containing active coke particles in the purification tower are conveyed to a third bubbling area, dust in the dust-containing active coke particles and the active coke particles are separated in the third bubbling area, the separated dust is conveyed to a dedusting device, the active coke particles obtained after separation enter a storage bin, and in the step, a bubbling medium is continuously conveyed to the third bubbling area, wherein the flowing speed of the bubbling medium is 0.8-1.5 m/s;
s80: the active coke particles in the storage bin are conveyed to a second bubbling area, the active coke particles output by the storage bin are subjected to secondary dedusting treatment in the second bubbling area, the treated dust is conveyed to dedusting equipment, the treated active coke particles are conveyed to a purification tower, and the step S10 is executed again;
the active coke dry method flue gas treatment method in the specific embodiment further includes step S90: supplemental activated coke is delivered to the third bubbling zone.
Specifically, in step S70, a third bubbling region is disposed in the third vertical pipe, the supplementary active coke is conveyed to the third bubbling region through a third chute, the size range of the third chute is 150-400 mm, the cross section of the third chute is square or circular, and an included angle between the third chute and the third vertical pipe is an acute angle and is 30-55 °.
In addition, the flow rate of the bubbling medium in this specific example was determined by specific calculation with reference to formulas 1 and 2 in the specific example.
Compared with the first specific embodiment, in the active coke dry-method flue gas treatment method in the first specific embodiment, when the regeneration tower breaks down, active coke particles can be conveyed into the purification tower through the storage bin, so that workers can repair the regeneration tower in time. Through adding supplementary active burnt to the storage silo, can effectively guarantee that the inside active burnt of system is sufficient to effectively guarantee the efficiency that the flue gas was handled.
Detailed description of the preferred embodiment
As shown in fig. 1, the present embodiment discloses an active coke dry-method flue gas treatment system, which includes a purification tower 4 for purifying flue gas and a regeneration tower 9 for regenerating active coke, an active coke moving bed is disposed in the purification tower 4, the purification tower 4 discharges active coke particles generated by mutual collision and friction between dust-containing active coke particles and active coke particle layers to a first conveyor 7 through a first discharge discharger, and the first conveyor 7 conveys the active coke particles to the regeneration tower 9. A first bubbling area 27-1 is arranged between the outlet of the first conveyor 7 and the inlet of the regeneration tower 9, the first bubbling area 27-1 is arranged in a first vertical pipeline, the outlet of the first conveyor 7 is communicated with the first vertical pipeline through a first chute 27-2, the size range of the first chute 27-2 is 150-400 mm, the cross section of the first chute is square or circular, the included angle between the first chute 27-2 and the first vertical pipeline is an acute angle, and the included angle range is 30-55 degrees. The piping located upstream of the first bubbling zone, i.e., the first dusty gas line 27-3 shown in fig. 1, communicates with the dust-removing device 20, and the piping located downstream of the first bubbling zone 27-1 communicates with the blower 25 through the first bubbling gas line 27, which is used to deliver the bubbling medium air 24 to the first bubbling zone 27-1.
In this embodiment, the regeneration tower 9 conveys the regenerated active coke particles to the purification tower 4 through the second conveyor 12, a screening device is arranged between an inlet of the second conveyor 12 and an outlet of the regeneration tower 9, specifically, the screening device is a vibrating screen 11, a first outlet of the vibrating screen 11 is communicated with the second conveyor 12, the vibrating screen 11 discharges the regenerated active coke particles with the particle size larger than the preset particle size into the second conveyor 12 through the first outlet, a second outlet of the vibrating screen 11 is communicated with the ash tank 22, and the vibrating screen 11 discharges the regenerated active coke particles with the particle size smaller than the preset particle size into the second conveyor 12 through the second outlet. A second bubbling area 26-1 is arranged between the outlet of the second conveyor 12 and the inlet of the purification tower 4, the second bubbling area 26-1 is arranged in a second vertical pipeline, the outlet of the second conveyor 12 is communicated with the second vertical pipeline through a second chute 26-2, the size range of the second chute is 150-400 mm, the cross section of the second chute is square or circular, the included angle between the second chute 26-2 and the second vertical pipeline is an acute angle, and the included angle range is 30-55 degrees. The piping located upstream of the second bubbling zone 26-1, i.e., the second dusty gas line 26-3 shown in fig. 1, communicates with the dust-removing means 20, and the piping located downstream of the second bubbling zone 26-1 communicates with the blower 25 through the second bubbling gas line 26, and the blower 25 is used to convey the bubbling medium air 24 to the second bubbling zone 26-1.
In the present embodiment, the flue gas outlet of the dust removing device 20 is communicated with the flue gas inlet of the purifying tower 4; the first conveyor 7 is communicated with the dust removal equipment 20 through the first dust removal pipeline 7-1, and the second conveyor 12 is communicated with the dust removal equipment 20 through the second dust removal pipeline 12-1, so that dust generated in the process of conveying the active coke by the conveyors can be conveyed to the dust removal equipment, the handling capacity of a bubbling area can be reduced, the bubbling energy consumption is further reduced, and the dust removal efficiency is improved.
Specifically, the flow velocity of the bubbling medium delivered by the fan to the first bubbling region 27-1 and the second bubbling region 26-1 is 0.8 to 1.5m/s, and the specific calculation manner of the flow velocity of the bubbling medium is shown in formulas 1 and 2 in the first embodiment.
A specific embodiment mode of the specific embodiment of the active coke dry method flue gas treatment system of the present specific embodiment is as follows:
the method comprises the following steps of enabling dust-containing flue gas 1 to enter a purification tower 4, retaining a part of smoke dust in the purification tower, discharging the other part of smoke dust and active coke particles in the purification tower to a first conveyor 7 through a first discharging discharger 6, conveying the dust-containing active coke particles to a first chute 27-2 by the first conveyor 7, conveying bubbling medium air 24 provided by a fan 25 to the lower end of a first bubbling area 27-1 through a first bubbling gas pipeline 27, bubbling the dust-containing active coke particles entering the first bubbling area 27-1 through the first chute 27-2 to realize separation, conveying dust to an inlet of a dust removal device 20 through a first dust-containing gas pipeline 27-3, enabling the active coke particles to enter a regeneration tower 9 through a second feeding discharger 8, and discharging the regenerated active coke to a vibrating screen 11 through a second discharging discharger 10, active coke small particles with the particle size of less than 2mm are screened and conveyed by a vibrating screen and enter an ash tank 22 through an ash discharge valve 13, active coke particles with the particle size of more than 2mm are conveyed to the lower end of a second bubbling area 26-1 through a second conveyor 12 and a second chute 26-2 at the upper end of a purification tower 4, bubbling medium air 24 provided by a fan 25 is conveyed to the lower end of the second bubbling area 26-1 through a second bubbling gas pipeline 26, dust-containing active coke particles entering the second bubbling area 26-2 through the second chute 26-2 are bubbled to realize separation, dust is conveyed to an inlet of a dust removal device 20 through a second dust-containing gas pipeline 26-3, the active coke particles enter an overhead bin 3 through a first feeding discharger 2 and then enter the purification tower 4, the active coke particles in the purification tower 4 purify dust-containing flue gas, are discharged through a first discharging discharger by means of self gravity, and pass through a material conveying system, so that a circulation process is realized. The dust-containing gas is conveyed to the dust removing device 20 through a first dust removing pipeline 7-1, a second dust removing pipeline 12-1, a second dust-containing gas pipeline 26-3 and a first dust-containing gas pipeline 27-3, the gas after dust removal is returned to a flue gas inlet through a dust collecting fan 23, and the collected dust is discharged into a dust tank 22 through a second dust discharging valve 21.
In the present embodiment, a bucket conveyor is used as the first conveyor 7 and the second conveyor 12, and a bucket conveyor is used as the third conveyor 17. First feeding tripper 2, second feeding tripper 8, second ejection of compact tripper 10 are the double-core tripper, and first ejection of compact tripper 6, third ejection of compact tripper 16 are the star type tripper. Of course, in other concrete implementation processes, first conveyer, second conveyer, third conveyer to and first feeding tripper, second feeding tripper, first ejection of compact tripper, second ejection of compact tripper, third ejection of compact tripper, fourth ejection of compact tripper all can choose other commonly used outsourcing to purchase the piece, and here is no longer repeated.
Active coke dry method flue gas treatment system in this embodimentCan improve on original system, and original system changes lessly, and simple structure, investment and working costs are lower, have efficient dust collection efficiency, can satisfy the dust and ultralow emission 5mg/Nm 3 The active coke particles can be recycled, and the waste of the active coke particles is avoided.
Of course, in other embodiments of the active coke dry flue gas treatment system of the present invention, the flue gas outlet of the dust removal device may not be communicated with the flue gas inlet of the purification tower, but directly discharge the flue gas; a dust removal pipeline is not required to be arranged between the conveyor and the dust removal equipment; the connecting structure of the conveyor and the bubbling area can be adjusted according to actual needs; in addition, the flow speed of the bubbling medium can be specifically set according to the requirement on the dust content of the exhaust gas, the particle size of the active coke particles and the particle size of the dust particles, and details are not repeated here.
Detailed description of the invention
As shown in fig. 2, compared with the third embodiment, the active coke-drying flue gas treatment system in the third embodiment further includes a storage bin 15 and a hopper 19, a feeding port of the storage bin 15 is communicated with a discharging port of the first conveyor 7, a third bubbling region 28-1 is disposed between the feeding port of the storage bin 19 and the discharging port of the first conveyor 7, a gate valve 14 is disposed on a communication pipeline between the first conveyor 7 and the third bubbling region 28-1, a pipeline located upstream of the third bubbling region 28-1, that is, a third dusty gas pipeline 28-3 shown in fig. 2 is communicated with the dust removal device 20, a pipeline located downstream of the third bubbling region 28-1 is communicated with a fan 25 through the third bubbling gas pipeline 28, the fan 25 conveys bubbling medium air 24 into the third bubbling region 28-1, and the flow speed of the bubbling medium air 24 is 0.8 to 1.5m/s, and the flow speed of the bubbling medium is calculated as shown in the first embodiment and the second embodiment 2.
Specifically, the charging hopper 19 conveys the supplementary active coke to the storage bin 15 through the third conveyor 17, and the discharge port of the third conveyor 17 is communicated with the feed inlet of the storage bin 15 through the third bubbling region 28-1. The third bubbling area 28-1 is specifically arranged in a third vertical pipeline, the outlet of the third conveyor 17 is communicated with the second vertical pipeline through a third chute 28-2, the size range of the third chute is 150-400 mm, the cross section of the third chute is square or circular, the included angle between the third chute 28-2 and the third vertical pipeline is an acute angle, and the included angle range is 30-55 degrees.
In the embodiment, the discharge port of the first conveyor 7 is communicated with the storage bin 15 through the third bubbling area 28-1, and the communication pipeline between the first conveyor 7 and the third bubbling area 28-1 is provided with the gate valve 14, when the regeneration tower can normally operate, the gate valve 14 is closed, and the first conveyor conveys the active coke particles and the dust-containing active coke particles into the regeneration tower through the first bubbling area. When the regeneration tower breaks down, the gate valve 14 is opened, the first conveyor 7 conveys the active coke particles and the dust-containing active coke particles to the storage bin 15 through the third bubbling area 28-1, and then the active coke particles are conveyed to the purification tower through the second conveyor, so that the regeneration tower can be maintained by workers in time.
The process of adding supplementary active coke in a specific application mode of the present embodiment is as follows; as shown in fig. 2, fresh active coke 18 is added into a hopper 19 and is conveyed to a third chute 28-2 through a third conveyor 17, bubbling medium air 24 provided by a fan 25 is conveyed to a downstream pipeline of a third bubbling area 28-1 through a third bubbling gas pipeline 28, dust-containing active coke particles entering the third bubbling area 28-1 through the third chute 28-2 are bubbled to realize separation, dust is conveyed to an inlet of a dust removing device 20 through a third dust-containing gas pipeline 28-3, the active coke particles enter a storage bin 15, and then fresh active coke is added to the circulating process through a third blanking discharger 16. The dust-containing gas is supplied to the dust removing device 20 through the third dust-containing gas line 28-3, and the dust removing process in the third embodiment is performed simultaneously.
The active coke dry processing system in the embodiment can not only solve the problem that a material conveying system cannot normally operate when a regeneration tower breaks down by arranging the storage bin, but also add supplementary active coke into the system through the charging hopper, thereby solving the active coke loss caused by chemical consumption and physical abrasion of the active coke, and ensuring the stable operation and the purification efficiency of the device.
It should be noted that the above embodiments can be freely combined as necessary. The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. An active coke dry method flue gas treatment method is characterized by comprising the following steps:
s10: the method comprises the following steps that (1) dust-containing flue gas enters a purification tower provided with an active coke particle layer, and the purification tower carries out dust removal treatment on the dust-containing flue gas;
s20: when the regeneration tower normally operates, active coke particles generated by mutual collision and friction between active coke particles containing dust in the purification tower and the active coke particle layer are conveyed to a first bubbling area through a first slide pipe, the first bubbling area is arranged in a first vertical pipeline, an included angle between the first vertical pipeline and the first slide pipe is an acute angle, dust and active coke particles in the active coke particles containing dust are separated in the first bubbling area, the separated dust is conveyed to a dedusting device, the separated active coke particles enter the regeneration tower, and in the step, a bubbling medium is continuously conveyed to the first bubbling area;
s30: the regeneration tower regenerates the active coke particles passing through the first bubbling zone to obtain regenerated active coke;
s40: screening the regenerated active coke, conveying the regenerated active coke with the particle size smaller than a preset particle size to an ash tank for storage, conveying the regenerated active coke with the particle size larger than the preset particle size to a second bubbling area through a second chute, wherein the second bubbling area is arranged in a second vertical pipeline, an included angle between the second vertical pipeline and the second chute is an acute angle, and in the step, continuously conveying a bubbling medium to the second bubbling area;
s50: and in the second bubbling area, separating the dust in the regenerated active coke with the particle size larger than the preset particle size from the regenerated active coke particles, conveying the separated dust to the dust removal equipment, feeding the separated regenerated active coke particles into the purification tower, and executing the step S10 again.
2. The active coke dry flue gas treatment method according to claim 1, characterized in that:
the active coke dry method flue gas treatment method further comprises the step S60: introducing the flue gas obtained after dust removal in the dust removal equipment into the purification tower; and/or;
in the step S20, the dust generated in the process that the activated coke particles and the dust-containing activated coke particles in the purification tower are conveyed to the first bubbling zone is conveyed to the dust removing device; and/or;
in the step S40, the dust generated in the process of conveying the regenerated active coke with the particle size larger than the preset particle size to the second bubbling region is conveyed to the dust removing device.
3. The active coke dry flue gas treatment method according to claim 1, characterized in that:
in the step S20, the flow rate of the bubbling medium is 0.8 to 1.5m/S; in step S40, the flow rate of the bubbling medium is 0.8 to 1.5m/S.
4. The active coke dry flue gas treatment method according to claim 1, characterized in that:
the method further comprises the following step after the step S10:
s70: when the regeneration tower breaks down, the active coke particles and the dust-containing active coke particles in the purification tower are conveyed to a third bubbling area, dust and active coke particles in the dust-containing active coke particles are separated in the third bubbling area, the separated dust is conveyed to a dust removal device, the active coke particles obtained after separation enter a storage bin, and in the step, a bubbling medium is continuously conveyed to the third bubbling area;
s80: and (2) conveying the active coke particles in the storage bin to the second bubbling area, performing secondary dust removal treatment on the active coke particles output by the storage bin in the second bubbling area, conveying the treated dust to the dust removal equipment, conveying the treated active coke particles to the purification tower, and executing the step S10 again.
5. The active coke dry flue gas treatment method according to claim 4, characterized in that:
further comprising step S90: supplemental activated coke is delivered to the third bubbling zone.
6. The utility model provides an active coke dry-process flue gas processing system, is including being used for purifying the purifying column of flue gas and being used for carrying out the regenerator column of regeneration to active coke, be equipped with active coke moving bed, its characterized in that in the purifying column:
the purification tower conveys active coke particles generated by mutual collision and friction between dust-containing active coke particles and active coke particle layers to the regeneration tower through a first conveyor, a first bubbling area is arranged between an outlet of the first conveyor and an inlet of the regeneration tower and is arranged in a first vertical pipeline, an outlet of the first conveyor is communicated with the first vertical pipeline through a first slide pipe, and an included angle between the first slide pipe and the first vertical pipeline is an acute angle;
the pipeline positioned at the upstream of the first bubbling zone is communicated with dust removing equipment, the pipeline positioned at the downstream of the first bubbling zone is communicated with a fan, and the fan is used for conveying a bubbling medium to the first bubbling zone;
the regeneration tower conveys the regenerated active coke particles to the purification tower through a second conveyor;
a screening device is arranged between an inlet of the second conveyor and an outlet of the regeneration tower, a first outlet of the screening device is communicated with the second conveyor, and a second outlet of the screening device is communicated with an ash tank;
a second bubbling area is arranged between the outlet of the second conveyor and the inlet of the purification tower, the second bubbling area is arranged in a second vertical pipeline, the outlet of the second conveyor is communicated with the second vertical pipeline through a second chute, and an included angle between the second chute and the second vertical pipeline is an acute angle;
and the pipeline positioned at the upstream of the second bubbling region is communicated with the dust removing equipment, the pipeline positioned at the downstream of the second bubbling region is communicated with a fan, and the fan is used for conveying a bubbling medium to the second bubbling region.
7. The active coke dry flue gas treatment system of claim 6, wherein:
the flue gas outlet of the dust removing equipment is communicated with the flue gas inlet of the purifying tower; and/or;
the first conveyor is communicated with the dust removal equipment through a first dust removal pipeline; and/or;
the second conveyor is communicated with the dust removal equipment through a second dust removal pipeline.
8. The active coke-drying flue gas treatment system of claim 6, wherein:
the flow speed of the bubbling medium conveyed to the first bubbling area and the second bubbling area by the fan is 0.8-1.5 m/s.
9. The active coke dry flue gas treatment system of claim 6,
further comprising: the material storage bin is characterized in that a feeding port of the material storage bin is communicated with a discharge port of the first conveyor, a third bubbling area is arranged between the feeding port of the material storage bin and the discharge port of the first conveyor, a valve is arranged on a communication pipeline between the first conveyor and the third bubbling area, a pipeline positioned on the upstream of the third bubbling area is communicated with the dust removal equipment, and a pipeline positioned on the downstream of the third bubbling area is communicated with the fan.
10. The active coke dry flue gas treatment system of claim 9,
further comprising: the active coke dry method flue gas treatment system further comprises a feeding hopper, the feeding hopper conveys supplementary active coke to the storage bin through a third conveyor, and a discharge port of the third conveyor is communicated with a feeding port of the storage bin through a third bubbling area.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711264855.5A CN107854924B (en) | 2017-12-05 | 2017-12-05 | Activated coke dry method flue gas treatment method and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711264855.5A CN107854924B (en) | 2017-12-05 | 2017-12-05 | Activated coke dry method flue gas treatment method and system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107854924A CN107854924A (en) | 2018-03-30 |
| CN107854924B true CN107854924B (en) | 2023-01-17 |
Family
ID=61704612
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711264855.5A Active CN107854924B (en) | 2017-12-05 | 2017-12-05 | Activated coke dry method flue gas treatment method and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107854924B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110975513A (en) * | 2019-11-29 | 2020-04-10 | 中冶南方都市环保工程技术股份有限公司 | Active coke desulfurization material circulation system |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5735921A (en) * | 1980-08-14 | 1982-02-26 | Kansai Coke & Chem Co Ltd | Purification of gas |
| US5034115A (en) * | 1990-04-27 | 1991-07-23 | Mobil Oil Corporation | Process and apparatus for fast fluidized bed regeneration of catalyst in a bubbling bed catalyst regenerator |
| US5346610A (en) * | 1992-12-30 | 1994-09-13 | Mobil Oil Corporation | Multi-stage regeneration of catalyst in a bubbling bed catalyst regenerator |
| JP2013202434A (en) * | 2012-03-27 | 2013-10-07 | Taiheiyo Cement Corp | Method for disposing of fluidized bed-system boiler ash and disposer |
| CN106178813A (en) * | 2016-07-08 | 2016-12-07 | 中山市道享节能技术服务有限公司 | A kind of coal high-efficiency clean utilization system based on activated coke dry FGD process technology |
| CN206243895U (en) * | 2016-10-10 | 2017-06-13 | 上海克硫环保科技股份有限公司 | A kind of elephant trunk and the integrated cleaning system of activated coke waste gas |
Family Cites Families (24)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2068771B (en) * | 1980-02-08 | 1984-05-16 | Coal Industry Patents Ltd | Fluidic switched fluid cleaning |
| DE3410895A1 (en) * | 1984-03-24 | 1985-10-03 | Perfluktiv-Consult AG, Basel | METHOD AND SYSTEM FOR REDUCING THE POLLUTANT CONTENT OF SMOKE GASES |
| US5141712A (en) * | 1990-04-27 | 1992-08-25 | Mobil Oil Corporation | Process and apparatus for fast fluidized bed regeneration of catalyst in a bubbling bed catalyst regenerator |
| JPH07116454A (en) * | 1993-10-21 | 1995-05-09 | Babcock Hitachi Kk | Process and device for desulfurizing exhaust gas |
| US5788944A (en) * | 1995-02-28 | 1998-08-04 | Babcock-Hitachi Kabushiki Kaisha | Wet-type flue gas desulfurization plant and method making use of a solid desulfurizing agent |
| JP3996968B2 (en) * | 1996-12-11 | 2007-10-24 | 千代田化工建設株式会社 | Flue gas desulfurization method and apparatus |
| WO2001032293A1 (en) * | 1999-11-02 | 2001-05-10 | Nkk Corporation | Exhaust gas dust collecting device |
| CN1204955C (en) * | 2002-01-29 | 2005-06-08 | 国家电站燃烧工程技术研究中心 | Cyclic fluidized bed active coke desulfurating and sulfur reutilization method |
| JP2003286020A (en) * | 2002-03-27 | 2003-10-07 | Electric Power Dev Co Ltd | Highly activated active coke powder and manufacturing method thereof |
| CN101007231A (en) * | 2006-12-25 | 2007-08-01 | 严雪林 | Purifying tower for setting machine |
| JP4838196B2 (en) * | 2007-05-17 | 2011-12-14 | 重英 可計 | Continuous regeneration type particulate matter filter |
| CN101721882A (en) * | 2009-12-15 | 2010-06-09 | 中电投远达环保工程有限公司 | Circulating cooling system for active coke dry-method desulfuration adsorption tower moving bed and method |
| CN101732948B (en) * | 2009-12-31 | 2012-10-03 | 中电投远达环保工程有限公司 | Three-stage integrated treatment system and method for purification and regeneration of activated coke flue gas |
| CN202438326U (en) * | 2012-02-24 | 2012-09-19 | 重庆康达环保产业（集团）有限公司 | Equipment for regenerating saturated activated coke |
| CN102580705B (en) * | 2012-02-29 | 2013-10-16 | 上海克硫环保科技股份有限公司 | Comprehensive heat energy utilizing type active coke purifying and regenerating process system and active coke purifying and regenerating process method |
| CN102716635A (en) * | 2012-06-12 | 2012-10-10 | 清华大学 | Method and system for simultaneously removing heavy metals and fine particle matters in smoke |
| CN102895839B (en) * | 2012-10-17 | 2014-10-22 | 田鹏程 | Device and method for performing integrated purification on smoke |
| CN104548809A (en) * | 2014-12-11 | 2015-04-29 | 南京工业大学 | Active coke desulfurization and denitrification and membrane separation dust removal integrated system and treatment method |
| CN105289204B (en) * | 2015-11-23 | 2018-05-15 | 金川集团股份有限公司 | A kind of system and method for powder activated burnt processing low concentration sulphur dioxide flue gas |
| CN205599176U (en) * | 2016-04-20 | 2016-09-28 | 杭州回水科技股份有限公司 | Be used for active burnt palingenetic equipment of granule |
| CN105771946B (en) * | 2016-05-16 | 2019-01-22 | 上海克硫环保科技股份有限公司 | A kind of active coke regeneration system and regeneration method |
| CN206424781U (en) * | 2016-09-23 | 2017-08-22 | 中冶华天南京工程技术有限公司 | Horizontal modularization flue gas desulfurization and denitrification absorption regeneration integral system |
| CN106635105B (en) * | 2016-12-07 | 2019-07-23 | 神华集团有限责任公司 | Activated coke preparation facilities and method |
| CN207591501U (en) * | 2017-12-05 | 2018-07-10 | 上海克硫环保科技股份有限公司 | A kind of activated coke dry method flue gas processing system |
-
2017
- 2017-12-05 CN CN201711264855.5A patent/CN107854924B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5735921A (en) * | 1980-08-14 | 1982-02-26 | Kansai Coke & Chem Co Ltd | Purification of gas |
| US5034115A (en) * | 1990-04-27 | 1991-07-23 | Mobil Oil Corporation | Process and apparatus for fast fluidized bed regeneration of catalyst in a bubbling bed catalyst regenerator |
| US5346610A (en) * | 1992-12-30 | 1994-09-13 | Mobil Oil Corporation | Multi-stage regeneration of catalyst in a bubbling bed catalyst regenerator |
| JP2013202434A (en) * | 2012-03-27 | 2013-10-07 | Taiheiyo Cement Corp | Method for disposing of fluidized bed-system boiler ash and disposer |
| CN106178813A (en) * | 2016-07-08 | 2016-12-07 | 中山市道享节能技术服务有限公司 | A kind of coal high-efficiency clean utilization system based on activated coke dry FGD process technology |
| CN206243895U (en) * | 2016-10-10 | 2017-06-13 | 上海克硫环保科技股份有限公司 | A kind of elephant trunk and the integrated cleaning system of activated coke waste gas |
Non-Patent Citations (1)
| Title |
|---|
| Process development of coke oven gas to methanol integrated with CO2 recycle for satisfactory techno-economic performance;Qun Yi et al.;《Energy》;20161031;第112卷;第618-628页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107854924A (en) | 2018-03-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101559323B (en) | Digestive circulating fluid bed flue gas desulfurization method and device | |
| CN108380041A (en) | A kind of coke oven flue gas system for desulfuration and denitration and method based on activated carbon/coke | |
| CN102580455A (en) | Sintering smoke treatment system and sintering smoke treatment method | |
| CN107998812B (en) | Pneumatic conveying system and pneumatic conveying method for activated carbon | |
| CN105080332A (en) | Resource utilization system for pellet sintering waste gas and method | |
| WO2016011682A1 (en) | Equipment and method for circulating fluidized bed semidry simultaneous desulfurization, denitration, demercuration, and removal of dioxins of sintering flue gas | |
| CN203886406U (en) | Tail gas purification device of circulating fluid bed garbage incinerator | |
| CN205796927U (en) | Reverse-flow integration activated coke smoke eliminator | |
| CN105289204A (en) | System and method using powdery active cock for processing low concentration sulfur dioxide flue gas | |
| CN202289850U (en) | Smoke burning disposal system for sludge | |
| CN205145970U (en) | Charcoal base catalyst SOx/NOx control system | |
| CN210495771U (en) | Activated carbon desulfurization and denitrification system capable of being comprehensively utilized | |
| CN102872675A (en) | Buffer, bypass device, and absorption tower and adsorption tower provided with bypass device | |
| CN107854924B (en) | Activated coke dry method flue gas treatment method and system | |
| CN204952658U (en) | Sintering pelletizing flue gas resource system | |
| CN207591501U (en) | A kind of activated coke dry method flue gas processing system | |
| CN207237616U (en) | Activated carbon air-transport system | |
| CN108325295B (en) | Method and device for separating fine particles in high-temperature gas by fluidized bed | |
| CN212157203U (en) | System for removing dioxin in waste incineration fly ash in parallel connection with cement clinker production line | |
| CN104667746B (en) | A kind of low-temperature circulating regenerates denitration catalyst device | |
| CN111991991A (en) | Active coke turbulent bed desulfurization tower, system and method | |
| CN202683026U (en) | Wet-method demercuration system | |
| CN115888374A (en) | Flue gas treatment system and method for breaking inner side wall effect of tower and improving pollutant removal efficiency | |
| CN207980821U (en) | A kind of mostly de- minimum discharge device of complexity flue gas activated coke | |
| CN212440685U (en) | Purification system for tail flue gas of cement kiln |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |