CN111991991A - Active coke turbulent bed desulfurization tower, system and method - Google Patents
Active coke turbulent bed desulfurization tower, system and method Download PDFInfo
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- CN111991991A CN111991991A CN202010719315.7A CN202010719315A CN111991991A CN 111991991 A CN111991991 A CN 111991991A CN 202010719315 A CN202010719315 A CN 202010719315A CN 111991991 A CN111991991 A CN 111991991A
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
- B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
- B01D53/12—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents according to the "fluidised technique"
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- 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
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
- B01D46/023—Pockets filters, i.e. multiple bag filters mounted on a common frame
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8628—Processes characterised by a specific catalyst
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2255/00—Catalysts
- B01D2255/70—Non-metallic catalysts, additives or dopants
- B01D2255/702—Carbon
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses an active coke turbulent bed desulfurization tower, a system and a method, wherein the active coke turbulent bed desulfurization tower comprises a cylindrical and vertically arranged tower body, the side wall of the bottom of the tower body is provided with a flue gas inlet, at least one group of turbulent bed parts are arranged in the tower body and positioned above the flue gas inlet, each turbulent bed part comprises a gas distribution plate and an overflow pipe, the edge of the gas distribution plate is connected with the inner wall of the tower body, the overflow pipe penetrates through the gas distribution plate, the lower opening of the overflow pipe of the lowest turbulent bed part penetrates through the bottom plate of the tower body, the side wall of the middle of the tower body is provided with an active coke inlet, the active coke inlet is positioned between the gas distribution plate of the highest turbulent bed part and the upper opening of the overflow pipe, and the top of the. The invention can improve the mass transfer in the desulfurization and denitrification process and improve the pollutant removal efficiency and the working sulfur capacity of the active coke.
Description
Technical Field
The invention belongs to the field of combustion flue gas pollutant removal, and relates to an active coke turbulent bed desulfurization tower, a system and a method.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
The active coke flue gas treatment technology utilizes the adsorption and catalysis functions of the active coke to ensure that SO in the flue gas2And H2O and O2Reaction to form H2SO4Storing the active coke in the active coke hole; make NOx and NH in the flue gas3Reduction reaction to generate N2And H2O; realize SO in flue gas2The method can realize the cooperative control of multiple pollutants such as VOCs, HCl, HF, Hg, dioxin and the like; meanwhile, the recycling of the active coke and the SO can be realized through the regeneration of the active coke2The resource recycling is a pollutant cooperative control technology with wide prospect.
At present, the desulfurization and denitrification technology of the active coke is popularized and applied in the steel, metallurgy and coking industries in a large scale, and granular formed active coke is adopted. The granular formed active coke has the problems of serious physical abrasion loss of granules, high use cost of the active coke, low use rate and the like in the process of removing pollutants by a moving bed. The powdered active coke is used for replacing granular formed active coke, so that the adsorption mass transfer process can be greatly improved, and meanwhile, the continuous control of the process can be realized in the fluidized bed reactor. The circulating fluidized bed (semi-) dry flue gas desulfurization system uses lime as desulfurization absorbent and uses circulating fluidized bed as reactor to reach high desulfurization efficiency, and has very high popularization rate in China. However, through the research of the inventor of the present invention, it is found that in the process of implementing desulfurization by using a circulating fluidized bed as a reactor and powdered activated coke as an adsorbent or a catalyst, it is difficult to obtain higher working sulfur capacity of the activated coke on the premise of ensuring desulfurization efficiency due to the shorter residence time of the activated coke.
Disclosure of Invention
In order to solve the defects of the prior art, the invention aims to provide an active coke turbulent bed desulfurization tower, an active coke turbulent bed desulfurization system and an active coke turbulent bed desulfurization method, which can improve mass transfer in the desulfurization and denitrification process and improve pollutant removal efficiency and working sulfur capacity of active coke.
In order to achieve the purpose, the technical scheme of the invention is as follows:
on one hand, the active coke turbulent bed desulfurization tower comprises a tower body, wherein the tower body is cylindrical and vertically arranged, a flue gas inlet is formed in the side wall of the bottom of the tower body, at least one group of turbulent bed parts are arranged in the tower body and positioned above the flue gas inlet, each turbulent bed part comprises a gas distribution plate and an overflow pipe, the edge of each gas distribution plate is connected with the inner wall of the tower body, each overflow pipe penetrates through the gas distribution plates, an opening below the overflow pipe of the lowest turbulent bed part penetrates through the bottom plate of the tower body, an active coke inlet is formed in the side wall of the middle of the tower body and positioned between the gas distribution plate of the highest turbulent bed part and the opening above the overflow pipe, and a gas phase outlet is;
when the turbulent bed parts are in a group, the lowest turbulent bed part and the highest turbulent bed part are both turbulent bed parts; when the turbulent bed parts are more than two groups, the turbulent bed parts are arranged in sequence from bottom to top, openings below overflow pipes of the upper turbulent bed part are positioned above the gas distribution plate of the lower turbulent bed part, the lowermost turbulent bed part is the uppermost turbulent bed part, and the uppermost turbulent bed part is the uppermost turbulent bed part.
In the active coke turbulent bed desulfurization tower provided by the invention, a tower body bottom plate and a gas distribution plate of a turbulent bed part form a flue gas space, flue gas enters the flue gas space through a flue gas inlet, and the flue gas in the flue gas space enters the upper part of the gas distribution plate under the action of the gas distribution plate and contacts with active coke to carry out adsorption or catalytic reaction. The overflow pipe penetrates through the gas distribution plate, the height of the overflow pipe, which is positioned on the gas distribution plate, is the height of a bed layer for reacting the active coke with the flue gas, the active coke which is in full contact with the flue gas is discharged or enters a turbulent bed part below the overflow pipe. The active burnt import sets up between the gas distribution board of upmost level turbulent bed part and overflow pipe top opening, aim at: 1. the active coke enters power to be matched with the flue gas for fluidization; 2. the active coke is mixed with the flue gas in the bed layer, and the phenomenon that the contact time of the active coke and the flue gas is too short and the active coke is discharged from an overflow pipe is avoided. The invention is provided with a plurality of groups of turbulent bed parts, so that the active coke can be contacted with the flue gas in the plurality of groups of turbulent bed parts, thereby further increasing the working sulfur capacity of the active coke.
On the other hand, the active coke turbulent bed desulfurization system comprises the active coke turbulent bed desulfurization tower, a powdery active coke feeding device, a dust removal device and a booster fan, wherein a feeding outlet of the powdery active coke feeding device is connected with an active coke inlet of the active coke turbulent bed desulfurization tower, an inlet of the dust removal device is connected with a gas phase outlet of the active coke turbulent bed desulfurization tower, and an outlet of the dust removal device is connected with an inlet of the booster fan.
The invention adds the booster fan, increases the flow speed of the flue gas, accelerates the internal fluidization speed of the turbulent bed part of the active coke turbulent bed desulfurization tower, and thus increases the contact efficiency of the flue gas and the active coke. The dust removal device is arranged between the booster fan and the active coke turbulent motion bed desulfurization tower, so that part of active coke can be prevented from being brought out at an excessively high flue gas speed.
And the flue gas enters the bottom of the active coke turbulent bed desulfurization tower from a flue gas inlet, enters the upper part of a gas distribution plate through the air distribution of the gas distribution plate, is fluidized above the gas distribution plate, so that the flue gas is contacted with the active coke to carry out adsorption or catalytic reaction, the reacted active coke enters the lower turbulent bed part through an overflow pipe to be contacted with the flue gas or is discharged through the overflow pipe, and the flue gas contacted with the active coke is dedusted and discharged.
The invention has the beneficial effects that:
1) the invention obtains higher desulfurization efficiency by controlling the state that the powdery active coke particles in the desulfurization tower are in the turbulent fluidized bed in the flue gas.
2) The invention can obtain higher grain retention time, thereby improving the working sulfur capacity of the desulfurization active coke.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic structural view of an activated coke turbulent bed desulfurization system provided in example 1 of the present invention;
FIG. 2 is a schematic structural diagram of an activated coke turbulent bed desulfurization system provided in example 2 of the present invention;
FIG. 3 is a schematic structural diagram of an activated coke turbulent bed desulfurization system provided in example 3 of the present invention;
FIG. 4 is a schematic structural diagram of an activated coke turbulent bed desulfurization system provided in example 4 of the present invention;
FIG. 5 is a histogram of sulfur capacity adsorbed by home-made activated coke;
FIG. 6 is a histogram of sulfur capacity adsorption of commercial activated coke;
the system comprises a turbulent bed desulfurization tower, a powdery active coke feeding system, a filtering type bag dust removal device, a booster fan, a turbulent bed desulfurization tower, an overflow pipe, a gas distribution plate, a circulating fluidized bed desulfurization tower, a cyclone separator, a circulating coke feeding system, a circulating ammonia spraying system and a circulating fluidized bed desulfurization tower, wherein the turbulent bed desulfurization tower comprises a flue gas inlet channel 1, the powdery active coke feeding system 2, the filtering type bag dust removal device 3, the booster fan 5, the turbulent bed desulfurization tower 5-1, the overflow pipe 5-2, the gas distribution plate 6, the circulating fluidized bed desulfurization tower flue gas inlet.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
The invention provides a desulfurization tower, a system and a method for active coke turbulent bed, which have the defect of short retention time of active coke when the existing circulating fluidized bed reactor is used for active coke adsorption or catalytic desulfurization.
The invention provides an active coke turbulent bed desulfurization tower, which comprises a tower body, wherein the tower body is cylindrical and vertically arranged, the side wall of the bottom of the tower body is provided with a flue gas inlet, at least one group of turbulent bed parts are arranged in the tower body, the turbulent bed parts are positioned above the flue gas inlet, each turbulent bed part comprises a gas distribution plate and an overflow pipe, the edge of the gas distribution plate is connected with the inner wall of the tower body, the overflow pipe penetrates through the gas distribution plate, the lower opening of the overflow pipe of the lowest turbulent bed part penetrates through the bottom plate of the tower body, the side wall of the middle of the tower body is provided with an active coke inlet, the active coke inlet is positioned between the gas distribution plate of the highest turbulent bed part and the upper opening of the overflow pipe, and the;
when the turbulent bed parts are in a group, the lowest turbulent bed part and the highest turbulent bed part are both turbulent bed parts; when the turbulent bed parts are more than two groups, the turbulent bed parts are arranged in sequence from bottom to top, openings below overflow pipes of the upper turbulent bed part are positioned above the gas distribution plate of the lower turbulent bed part, the lowermost turbulent bed part is the uppermost turbulent bed part, and the uppermost turbulent bed part is the uppermost turbulent bed part.
In the active coke turbulent bed desulfurization tower provided by the invention, a tower body bottom plate and a gas distribution plate of a turbulent bed part form a flue gas space, flue gas enters the flue gas space through a flue gas inlet, and the flue gas in the flue gas space enters the upper part of the gas distribution plate under the action of the gas distribution plate and contacts with active coke to carry out adsorption or catalytic reaction. The overflow pipe penetrates through the gas distribution plate, the height of the overflow pipe, which is positioned on the gas distribution plate, is the height of a bed layer for reacting the active coke with the flue gas, the active coke which is in full contact with the flue gas is discharged or enters a turbulent bed part below the overflow pipe. The active burnt import sets up between the gas distribution board of upmost level turbulent bed part and overflow pipe top opening, aim at: 1. the active coke enters power to be matched with the flue gas for fluidization; 2. the active coke is mixed with the flue gas in the bed layer, and the phenomenon that the contact time of the active coke and the flue gas is too short and the active coke is discharged from an overflow pipe is avoided. The invention is provided with a plurality of groups of turbulent bed parts, so that the active coke can be contacted with the flue gas in the plurality of groups of turbulent bed parts, thereby further increasing the working sulfur capacity of the active coke.
In some examples of this embodiment, the turbulent bed part has an outlet above the overflow pipe and a distance of 0.3-2 m from the gas distribution plate.
In some examples of this embodiment, the vertical distance between the active coke inlet and the opening above the overflow pipe of the turbulent bed part at the uppermost stage is 0.4-1 m.
In some embodiments of this embodiment, the gas distribution plate is a perforated plate or a hood plate.
In one or more embodiments, when a group of turbulent bed components are arranged inside the tower body, the gas distribution plate is a hood wind distribution plate;
when two or more groups of turbulent bed parts are arranged in the tower body, the gas distribution plate of the lowest turbulent bed part is a hood wind distribution plate, and the gas distribution plates of other turbulent bed parts are porous plates.
In some embodiments of this embodiment, a gas flow guide is disposed below the gas distribution plate of the lowest turbulent bed section. The reasonable gas uniform distribution structure ensures that the flue gas passing through the first-stage gas distribution plate uniformly passes through the first-stage gas distribution plate.
In some embodiments of this embodiment, the two or more sets of turbulent bed sections are disposed within the column body such that the diameter of the column body between two adjacent gas distribution plates is different from the diameter of the column body between two other adjacent gas distribution plates. To obtain different superficial gas velocities.
In some examples of this embodiment, a sparger is mounted within the column, the inlet of the sparger being configured for connection to a source of ammonia gas.
The invention also provides an active coke turbulent bed desulfurization system, which comprises the active coke turbulent bed desulfurization tower, a powdery active coke feeding device, a dust removal device and a booster fan, wherein a feeding outlet of the powdery active coke feeding device is connected with an active coke inlet of the active coke turbulent bed desulfurization tower, an inlet of the dust removal device is connected with a gas phase outlet of the active coke turbulent bed desulfurization tower, and an outlet of the dust removal device is connected with an inlet of the booster fan.
The invention adds the booster fan, increases the flow speed of the flue gas, accelerates the internal fluidization speed of the turbulent bed part of the active coke turbulent bed desulfurization tower, and thus increases the contact efficiency of the flue gas and the active coke. The dust removal device is arranged between the booster fan and the active coke turbulent motion bed desulfurization tower, so that part of active coke can be prevented from being brought out at an excessively high flue gas speed.
In some embodiments of this embodiment, the feeding device of the powdered activated coke feeding system is one or more of a star feeder, a screw feeder, or a loop feed valve connected in series with an air chute feeder.
In some embodiments of this embodiment, the dust removal device is a cyclone, a bag-type dust collector, or a series connection of both. The cyclone dust collector can be a first-stage cyclone dust collector or a multi-stage cyclone dust collector.
Some examples of this embodiment include a circulating fluidized bed desulfurization tower having a gas phase outlet connected to a flue gas inlet of an active coke turbulent bed desulfurization tower.
In one or more embodiments, the opening below the overflow pipe of the lowest turbulent bed part of the active coke turbulent bed desulfurization tower is connected with the active coke inlet of the circulating fluidized bed desulfurization tower.
In one or more embodiments, a dust removal device is connected between the active coke turbulent bed desulfurization tower and the circulating fluidized bed desulfurization tower.
Some examples of the embodiment include an ammonia spraying device, wherein the ammonia spraying device comprises an ammonia gas source and a nozzle, the nozzle is installed in the active coke turbulent bed desulfurization tower, and the inlet of the nozzle is connected with the ammonia gas source.
According to the third embodiment of the invention, the active coke turbulent bed desulfurization method is provided, the active coke turbulent bed desulfurization tower or the active coke turbulent bed desulfurization system is provided, the flue gas enters the bottom of the active coke turbulent bed desulfurization tower from the flue gas inlet, the air distributed through the gas distribution plate enters the upper part of the gas distribution plate, the flue gas and the active coke are fluidized above the gas distribution plate, so that the flue gas is contacted with the active coke for adsorption or catalytic reaction, the reacted active coke enters the lower turbulent bed part through the overflow pipe to be contacted with the flue gas, or is discharged through the overflow pipe, and the flue gas contacted with the active coke is dedusted and discharged.
The active coke in the invention is powdery active coke. In some examples of this embodiment, the particle size of the activated coke is 0.03 to 1 mm.
In some examples of the embodiment, the flow velocity of the flue gas in the active coke turbulent bed desulfurization tower is 0.1-2 m/s.
In order to make the technical solutions of the present invention more clearly understood by those skilled in the art, the technical solutions of the present invention will be described in detail below with reference to specific embodiments.
Example 1
An active coke turbulent bed desulfurization system is shown in figure 1 and comprises a turbulent bed desulfurization tower flue gas inlet channel 1, a powdery active coke feeding system 2, a filtering type cloth bag dust removal device 3, a booster fan 4 and a turbulent bed desulfurization tower 5; wherein the turbulent bed desulfurizing tower 5 comprises an overflow pipe 5-1 and a gas distribution plate 5-2.
The turbulent bed desulfurization tower flue gas inlet channel 1 is connected with the bottom of the turbulent bed desulfurization tower 5, the top of the turbulent bed desulfurization tower 5 is connected with the filtering type cloth bag dust removing device 3, and the outlet of the filtering type cloth bag dust removing device 3 is connected with the booster fan 4 through a flue gas pipeline. The powdery active coke feeding system 2 is connected with the turbulent bed desulfurizing tower.
Fresh powdery active coke is fed into a turbulent bed desulfurization tower 5 through a powdery active coke feeding system 2, flue gas enters the bottom of the turbulent bed desulfurization tower 5 through a flue gas inlet channel 1 of the turbulent bed desulfurization tower, and is mixed with active coke particles through a gas distribution plate 5-2 to form a turbulent fluidized bed. With the increase of the amount of the active coke fed by the powdery active coke feeding system 2, when the height of the bed layer exceeds the top end of the overflow pipe 5-1, the active coke particles are discharged out of the turbulent bed desulfurizing tower 5 through the overflow pipe 5-1, and the discharged active coke particles can be recycled after regeneration. After passing through the bed layer particles, the flue gas is separated from the carried active coke particles at the filtering type cloth bag dust removing device 3 and then is discharged by a booster fan 4.
Example 2
An active coke turbulent bed desulfurization system is shown in figure 2 and comprises a turbulent bed desulfurization tower flue gas inlet channel 1, a powdery active coke feeding system 2, a filtering type cloth bag dust removal device 3, a booster fan 4 and a turbulent bed desulfurization tower 5; wherein the turbulent bed desulfurizing tower 5 comprises three overflow pipes 5-1 and three gas distribution plates 5-2.
The turbulent bed desulfurization tower flue gas inlet channel 1 is connected with the bottom of the turbulent bed desulfurization tower 5, the top of the turbulent bed desulfurization tower 5 is connected with the filtering type cloth bag dust removing device 3, and the outlet of the filtering type cloth bag dust removing device 3 is connected with the booster fan 4 through a flue gas pipeline. The powdery active coke feeding system 2 is connected with the turbulent bed desulfurizing tower.
The flue gas enters the bottom of a turbulent bed desulfurization tower 5 through a flue gas inlet channel 1 of the turbulent bed desulfurization tower, is mixed with active coke particles through a first-stage blast cap distribution plate at the bottommost part of a gas distribution plate 5-2 to form a first-stage turbulent fluidized bed, and then sequentially passes through two upper-stage pore plate distribution plates to form a third-stage turbulent bed. After passing through the bed layer particles, the flue gas is separated from the carried active coke particles at the filtering type cloth bag dust removing device 3 and then is discharged by a booster fan 4. Fresh powdery active coke is fed into the uppermost turbulent bed of the turbulent bed desulfurization tower 5 through the powdery active coke feeding system 2, along with the increase of the amount of the active coke fed by the powdery active coke feeding system 2, when the height of a bed layer exceeds the top end of an overflow pipe 5-1, active coke particles are discharged through the overflow pipe 5-1 and are fed into the lower turbulent bed, finally, the active coke particles are discharged out of the turbulent bed desulfurization tower 5 through the overflow pipe of the lowermost turbulent bed, and the discharged active coke particles can be recycled after regeneration.
Example 3
An active coke turbulent bed desulfurization system is shown in figure 3 and comprises a circulating fluidized bed desulfurization tower flue gas inlet channel 6, a circulating fluidized bed desulfurization tower 7, a cyclone separator 8, a booster fan 4, a filtering type cloth bag dust removal device 3, a powdery active coke feeding system 2, a turbulent bed desulfurization tower 5, a turbulent bed desulfurization tower flue gas inlet channel 1 and a circulating coke feeding system 9; wherein the turbulent bed desulfurizing tower 5 comprises two overflow pipes 5-1 and two gas distribution plates 5-2.
The circulating fluidized bed desulfurization tower flue gas inlet channel 6 is connected with the bottom of the circulating fluidized bed desulfurization tower 7, the top of the circulating fluidized bed desulfurization tower 7 is connected with the cyclone separator 8, the outlet of the cyclone separator 8 is connected with the turbulent bed desulfurization tower flue gas inlet channel 1 through a flue gas pipeline, the turbulent bed desulfurization tower flue gas inlet channel 1 is connected with the bottom of the turbulent bed desulfurization tower 5, the top of the turbulent bed desulfurization tower 5 is connected with the filtering bag dust collector 3, and the outlet of the filtering bag dust collector 3 is connected with the booster fan 4 through a flue gas pipeline. The powdery active coke feeding system 2 is connected with the turbulent bed desulfurizing tower 5.
The original flue gas enters the bottom of a circulating fluidized bed desulfurization tower 7 through a flue gas inlet channel 6 of the circulating fluidized bed desulfurization tower, enters a flue gas inlet channel 1 of a turbulent bed desulfurization tower through a cyclone separator 8 connected with the top, is mixed with active coke particles through a first-stage distribution plate at the bottommost of a gas distribution plate 5-2 to form a first-stage turbulent fluidized bed, and then forms a second-stage turbulent bed through a first-stage orifice distribution plate above the first-stage turbulent fluidized bed. After passing through the bed layer particles, the flue gas is separated from the carried active coke particles at the filtering type cloth bag dust removing device 3 and then is discharged by a booster fan 4. Fresh powdery active coke is fed into the uppermost turbulent bed of the turbulent bed desulfurization tower 5 through the powdery active coke feeding system 2, along with the increase of the amount of the active coke fed by the powdery active coke feeding system 2, when the height of a bed layer exceeds the top end of an overflow pipe 5-1, active coke particles are discharged through the overflow pipe 5-1 and are fed into the lower turbulent bed, finally the active coke particles are discharged out of the turbulent bed desulfurization tower 5 through the overflow pipe of the lowermost turbulent bed and are conveyed to a connected circulating fluidized bed desulfurization tower 7, the active coke in the circulating fluidized bed desulfurization tower enters a cyclone separator 8 under the carrying of flue gas, after separation, one part of the active coke is fed back to the circulating fluidized bed desulfurization tower 7, and the other part of the active coke particles is discharged out of the desulfurization tower, and the discharged active coke particles can be fed back to the powdery active coke feeding system 2 for recycling.
Example 4
An active coke turbulent bed desulfurization system is shown in figure 4 and comprises a turbulent bed desulfurization tower flue gas inlet channel 1, an ammonia spraying system 10, a powdery active coke feeding system 2, a filtering type cloth bag dust removal device 3, a booster fan 4 and a turbulent bed desulfurization tower 5; wherein the turbulent bed desulfurizing tower 5 comprises three overflow pipes 5-1 and three gas distribution plates 5-2.
The turbulent bed desulfurization tower flue gas inlet channel 1 is connected with the bottom of the turbulent bed desulfurization tower 5, the top of the turbulent bed desulfurization tower 5 is connected with the filtering type cloth bag dust removing device 3, and the outlet of the filtering type cloth bag dust removing device 3 is connected with the booster fan 4 through a flue gas pipeline. The powdery active coke feeding system 2 is connected with the turbulent bed desulfurization tower 5, and the ammonia spraying system 10 is connected with the turbulent bed desulfurization tower 5.
The flue gas enters the bottom of a turbulent bed desulfurization tower 5 through a flue gas inlet channel 1 of the turbulent bed desulfurization tower, is mixed with active coke particles through a first-stage blast cap distribution plate at the bottommost part of a gas distribution plate 5-2 to form a first-stage turbulent fluidized bed, and then sequentially passes through two upper-stage pore plate distribution plates to form a third-stage turbulent bed. After passing through the bed layer particles, the flue gas is separated from the carried active coke particles at the filtering type cloth bag dust removing device 3 and then is discharged by a booster fan 4. Fresh powdery active coke is fed into the uppermost turbulent bed of the turbulent bed desulfurization tower 5 through the powdery active coke feeding system 2, along with the increase of the amount of the active coke fed by the powdery active coke feeding system 2, when the height of a bed layer exceeds the top end of an overflow pipe 5-1, active coke particles are discharged through the overflow pipe 5-1 and are fed into the lower turbulent bed, finally, the active coke particles are discharged out of the turbulent bed desulfurization tower 5 through the overflow pipe of the lowermost turbulent bed, and the discharged active coke particles are regenerated and then fed back to the powdery active coke feeding system 2 for recycling. The ammonia spraying system 10 sprays ammonia gas into the upper part of the second-stage turbulent bed of the turbulent bed desulfurization tower 5, and the ammonia gas and the flue gas are mixed and then pass through the upper-stage turbulent bed layer, so that nitrogen oxides in the flue gas can be reduced and removed under the catalytic action of active coke particles.
The sulfur adsorption capacity test is carried out on the self-made active coke and the commercial active coke, the results are shown in fig. 5-6, and the research shows that the retention time of the active coke influences the working sulfur capacity of the active coke, the sulfur capacities of the two active cokes are 14.58 mg/g and 4.05mg/g respectively in 5 minutes, and the sulfur adsorption capacities of the two active cokes are gradually increased along with the increase of the time. Meanwhile, the research finds that the average retention time of the coke breeze in the circulating fluidized bed is less than 5 minutes, while the retention time of the active coke turbulent bed desulfurization system provided by the application is 30-120 minutes, taking example 1 as an example, the retention time of the active coke is not 30 minutes, and the sulfur capacity of the two active cokes is 42.25 mg/g and 19.11mg/g respectively; compared with a circulating fluidized bed, the sulfur capacity of the active coke is obviously improved.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. An active coke turbulent bed desulfurization tower is characterized by comprising a tower body, wherein the tower body is cylindrical and vertically arranged, a flue gas inlet is formed in the side wall of the bottom of the tower body, at least one group of turbulent bed parts are arranged inside the tower body and positioned above the flue gas inlet, each turbulent bed part comprises a gas distribution plate and an overflow pipe, the edge of each gas distribution plate is connected with the inner wall of the tower body, each overflow pipe penetrates through each gas distribution plate, an opening below the overflow pipe of the lowest turbulent bed part penetrates through the bottom plate of the tower body, an active coke inlet is formed in the side wall of the middle of the tower body and positioned between the gas distribution plate of the highest turbulent bed part and the opening above the overflow pipe, and a gas phase outlet is formed;
when the turbulent bed parts are in a group, the lowest turbulent bed part and the highest turbulent bed part are both turbulent bed parts; when the turbulent bed parts are more than two groups, the turbulent bed parts are arranged in sequence from bottom to top, openings below overflow pipes of the upper turbulent bed part are positioned above the gas distribution plate of the lower turbulent bed part, the lowermost turbulent bed part is the uppermost turbulent bed part, and the uppermost turbulent bed part is the uppermost turbulent bed part.
2. The active coke turbulent bed desulfurization tower according to claim 1, wherein in the turbulent bed part, the distance between the outlet above the overflow pipe and the gas distribution plate is 0.3-2 m;
or the vertical distance between the active coke inlet and the opening above the overflow pipe of the uppermost turbulent bed part is 0.4-1 m.
3. The active coke turbulent bed desulfurization tower of claim 1, wherein said gas distribution plate is a perforated plate or a hood plate;
preferably, when a group of turbulent bed components are arranged in the tower body, the gas distribution plate is a hood wind distribution plate;
when two or more groups of turbulent bed parts are arranged in the tower body, the gas distribution plate of the lowest turbulent bed part is a hood wind distribution plate, and the gas distribution plates of other turbulent bed parts are porous plates.
4. The active turbulent fluidized bed desulfurizing tower as claimed in claim 1, wherein when two or more groups of turbulent fluidized bed units are set inside the tower body, the diameter of the tower body between two adjacent gas distributing plates is different from the diameter of the tower body between two other adjacent gas distributing plates.
5. The active turbulent coking bed desulfurization tower of claim 1 wherein a sparger is mounted within the tower body, the inlet of the sparger being configured for connection to a source of ammonia gas.
6. An active coke turbulent bed desulfurization system, characterized by comprising the active coke turbulent bed desulfurization tower of claim 1, a powdery active coke feeding device, a dust removal device and a booster fan, wherein a feeding outlet of the powdery active coke feeding device is connected with an active coke inlet of the active coke turbulent bed desulfurization tower, an inlet of the dust removal device is connected with a gas phase outlet of the active coke turbulent bed desulfurization tower, and an outlet of the dust removal device is connected with an inlet of the booster fan.
7. The system of claim 6, comprising a circulating fluidized bed desulfurization tower, wherein the gas phase outlet of the circulating fluidized bed desulfurization tower is connected to the flue gas inlet of the active coke turbulent bed desulfurization tower;
preferably, an opening below an overflow pipe of a turbulent bed part at the lowest stage of the active coke turbulent bed desulfurization tower is connected with an active coke inlet of the circulating fluidized bed desulfurization tower;
preferably, a dust removal device is connected between the active coke turbulent bed desulfurization tower and the circulating fluidized bed desulfurization tower.
8. The system of claim 6, comprising an ammonia injection device, wherein the ammonia injection device comprises an ammonia source and a nozzle, the nozzle is installed in the desulfurization tower of the turbulent bed of the activated coke, and an inlet of the nozzle is connected with the ammonia source.
9. A desulfurization method of an active coke turbulent bed is characterized in that an active coke turbulent bed desulfurization tower of claim 1 or an active coke turbulent bed desulfurization system of claim 6 is provided, flue gas enters the bottom of the active coke turbulent bed desulfurization tower from a flue gas inlet, air is distributed through a gas distribution plate and enters the upper part of the gas distribution plate, the flue gas and the active coke are fluidized above the gas distribution plate, the flue gas is contacted with the active coke to carry out adsorption or catalytic reaction, the reacted active coke enters a lower turbulent bed part through an overflow pipe to be contacted with the flue gas or is discharged through the overflow pipe, and the flue gas contacted with the active coke is dedusted and discharged.
10. The turbulent active coke bed desulfurization method according to claim 9, wherein the flow velocity of the flue gas in the turbulent active coke bed desulfurization tower is 0.1 to 2 m/s.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112675698A (en) * | 2020-12-23 | 2021-04-20 | 山东祥桓环境科技有限公司 | Desulfurization, denitrification and dust removal device of turbulent bed in separate bin and process thereof |
| US20220401968A1 (en) * | 2021-06-22 | 2022-12-22 | Foremost Equipment LP | Multicyclone separator |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0142603A1 (en) * | 1983-08-27 | 1985-05-29 | DORNIER SYSTEM GmbH | Apparatus for concentrating liquid solutions |
| CN105727708A (en) * | 2016-02-29 | 2016-07-06 | 中国科学院过程工程研究所 | Multi-layer fluidized bed two-stage activated carbon/coke flue gas simultaneous-desulfurization and denitrification system and method |
| CN108144443A (en) * | 2018-02-05 | 2018-06-12 | 山东大学 | A kind of powdered activated coke combined desulfurization and the system and method for denitration |
-
2020
- 2020-07-23 CN CN202010719315.7A patent/CN111991991A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0142603A1 (en) * | 1983-08-27 | 1985-05-29 | DORNIER SYSTEM GmbH | Apparatus for concentrating liquid solutions |
| CN105727708A (en) * | 2016-02-29 | 2016-07-06 | 中国科学院过程工程研究所 | Multi-layer fluidized bed two-stage activated carbon/coke flue gas simultaneous-desulfurization and denitrification system and method |
| CN108144443A (en) * | 2018-02-05 | 2018-06-12 | 山东大学 | A kind of powdered activated coke combined desulfurization and the system and method for denitration |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112675698A (en) * | 2020-12-23 | 2021-04-20 | 山东祥桓环境科技有限公司 | Desulfurization, denitrification and dust removal device of turbulent bed in separate bin and process thereof |
| CN112675698B (en) * | 2020-12-23 | 2023-02-28 | 山东祥桓环境科技有限公司 | Desulfurization, denitrification and dust removal device of turbulent bed in separate bin and process thereof |
| US20220401968A1 (en) * | 2021-06-22 | 2022-12-22 | Foremost Equipment LP | Multicyclone separator |
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