CN106693603B - Activated carbon method flue gas purification device and flue gas purification method - Google Patents

Activated carbon method flue gas purification device and flue gas purification method Download PDF

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CN106693603B
CN106693603B CN201510780033.7A CN201510780033A CN106693603B CN 106693603 B CN106693603 B CN 106693603B CN 201510780033 A CN201510780033 A CN 201510780033A CN 106693603 B CN106693603 B CN 106693603B
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activated carbon
chamber
flue gas
chambers
adsorption tower
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CN106693603A (en
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叶恒棣
魏进超
刘昌齐
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Zhongye Changtian International Engineering Co Ltd
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Zhongye Changtian International Engineering Co Ltd
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Priority to CN201510780033.7A priority Critical patent/CN106693603B/en
Priority to KR1020187013588A priority patent/KR102053559B1/en
Priority to PCT/CN2016/105451 priority patent/WO2017080502A1/en
Priority to RU2018117492A priority patent/RU2697688C1/en
Priority to BR112018009430-7A priority patent/BR112018009430B1/en
Priority to MYPI2018701431A priority patent/MY192747A/en
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    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • 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
    • B01D53/04—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 stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • 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
    • B01D53/04—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 stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0423—Beds in columns
    • 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
    • B01D46/0027—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions
    • B01D46/0036—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions by adsorption or absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • 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
    • B01D53/04—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 stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/206—Organic halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602

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  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
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  • Treating Waste Gases (AREA)
  • Separation Of Gases By Adsorption (AREA)

Abstract

The device comprises an active carbon adsorption tower, wherein the active carbon adsorption tower comprises an active carbon bed part (A), an active carbon bed part (B) and a transition zone (C) between the two parts, the active carbon adsorption tower comprises a feeding bin (3) positioned above the adsorption tower, a flue gas inlet (1) positioned at the lower part of the adsorption tower and a flue gas outlet (2) positioned at the upper part of the adsorption tower, a flue gas outflow end (G2) of the active carbon bed part (A) is communicated with a flue gas inlet end (G3) of the active carbon bed part (B) through a flue gas channel (5), the active carbon bed part (A) is provided with 2-7 active carbon chambers isolated by a porous partition plate (4), the thicknesses of the active carbon chambers positioned at the lower part are sequentially thickened along the flow direction of flue gas, and the active carbon bed part (B) is provided with 2-7 active carbon chambers isolated by the porous partition plate (4) and the thicknesses of the active carbon chambers positioned at the upper part are sequentially thickened along the flow direction of the flue gas.

Description

Activated carbon method flue gas purification device and flue gas purification method
Technical Field
The utility model relates to an activated carbon method flue gas purification device and a flue gas purification method, and belongs to the activated carbon method flue gas purification device suitable for treating atmospheric pollution, relating to the field of environmental protection.
Background
For industrial flue gas, especially sintering machine flue gas in the steel industry, it is desirable to employ desulfurization and denitrification apparatuses and processes including activated carbon adsorption towers and analytical towers. In a desulfurization and denitrification apparatus including an activated carbon adsorption tower for adsorbing pollutants including sulfur oxides, nitrogen oxides and dioxins from sintering flue gas or exhaust gas (particularly sintering flue gas of a sintering machine in the iron and steel industry) and a desorption tower for thermal regeneration of activated carbon.
The active carbon desulfurization has the advantages of high desulfurization rate, capability of simultaneously realizing denitration, dioxin removal, dust removal, no waste water and waste residue generation and the like, and is a flue gas purification method with great prospect. The activated carbon can be regenerated at high temperature, and sulfur oxides, nitrogen oxides, dioxin and other pollutants adsorbed on the activated carbon are rapidly resolved or decomposed (sulfur dioxide is resolved, and nitrogen oxides and dioxin are decomposed) at the temperature higher than 350 ℃. And as the temperature increases, the regeneration rate of the activated carbon further increases and the regeneration time shortens, preferably the regeneration temperature of the activated carbon in the desorption column is generally controlled to be about 430 c, so that the desired desorption temperature (or regeneration temperature) is, for example, in the range of 390-450 c, more preferably in the range of 400-440 c.
A conventional activated carbon desulfurization process is shown in fig. 1. The flue gas is introduced into an adsorption tower by a booster fan, and mixed gas of ammonia and air is sprayed into a tower inlet so as to improve NO X The purified flue gas enters a sintering main chimney for emission. Activated carbon is added into the adsorption tower from the top of the tower and moves downwards under the action of gravity and a discharging device at the bottom of the tower. Activated carbon coming out of the analysis tower is conveyed to an adsorption tower by a No. 2 activated carbon conveyor, the activated carbon saturated by the adsorption tower is discharged from the bottom, and the discharged activated carbon is conveyed to the analysis tower by a No. 1 activated carbon conveyor for activated carbon regeneration.
The function of the analytic tower is to adsorb SO from the activated carbon 2 Releasing, decomposing dioxin by over 80% at 400 deg.C and a certain residence time, cooling, sieving and reusing the activated carbon. Released SO 2 Can prepare sulfuric acid, etc., and the resolved active carbon is sent to an adsorption tower through a conveying device to be reused for adsorbing SO 2 And NO X Etc.
NO in adsorption column and desorption column X React with ammonia to remove NO by SCR, SNCR, etc X . The dust is adsorbed by the active carbon when passing through the adsorption tower, the vibrating screen at the bottom end of the analysis tower is separated, and the active carbon powder below the screen is sent to an ash bin and then can be sent to a blast furnace or sintered for use as fuel.
The flue gas is purified by adopting an activated carbon method, so that the flue gas can pass through a plurality of activated carbon beds in order to improve the purification effect. The multi-layered activated carbon bed arrangement is largely divided into an up-down structure and a front-back structure, as shown in fig. 2. The active carbon bed layer in the tower is a whole, and the active carbon moves down evenly by utilizing gravity. Along the flow direction of the flue gas, the activated carbon contacted with the flue gas firstly adsorbs more pollutants in the flue gas, and is discharged together with the following activated carbon, so that the following activated carbon is discharged into the tower without adsorption saturation or the preceding activated carbon is saturated and still does not play a flue gas purifying effect in the tower.
The prior art adopts an adsorption tower with a tandem structure, as shown in fig. 3, but a set of activated carbon conveying devices are added, so that not only are the investment and the operation cost increased, but also additional equipment maintenance workload is increased.
Therefore, in order to save investment and running cost and improve purification effect, a more reasonable activated carbon purification device is required.
Disclosure of Invention
The object of the present utility model is to provide an activated carbon process flue gas cleaning device comprising an activated carbon adsorption column comprising a lower activated carbon bed section (a), an upper activated carbon bed section (B) and a transition zone (C) between the two sections, and comprising a feed bin (3) above or on top of the adsorption column, a flue gas inlet (1) in the lower part of the adsorption column and a flue gas outlet (2) in the upper part of the adsorption column, wherein the flue gas outflow end (G2) of the lower activated carbon bed section (a) communicates with the flue gas inlet end (G3) of the upper activated carbon bed section (B) through a flue gas channel (5), the lower activated carbon bed section (a) having 2-7 (preferably 3-5) activated carbon chambers separated by a porous partition (4), the upper activated carbon bed section (B) having 2-7 (preferably 3-5) activated carbon chambers separated by a porous partition (4).
Preferably, the present utility model provides an activated carbon process flue gas cleaning apparatus comprising an activated carbon adsorption column (i.e., a desulfurization, denitrification apparatus comprising an activated carbon adsorption column and a desorption column or an activated carbon process flue gas cleaning apparatus comprising an activated carbon adsorption column and a desorption column), the activated carbon adsorption column comprising a lower activated carbon bed portion (A), an upper activated carbon bed portion (B) and a transition zone (C) (or referred to as an intermediate zone (C)) between the two portions, and the activated carbon adsorption tower comprises a feeding bin (3) positioned above or at the top of the adsorption tower, a flue gas inlet (1) positioned at the lower part of the adsorption tower and a flue gas outlet (2) positioned at the upper part of the adsorption tower, wherein a flue gas outflow end (G2) of the lower activated carbon bed part (A) is communicated with a flue gas inlet end (G3) of the upper activated carbon bed part (B) through a flue gas channel (5), the lower activated carbon bed part (A) is provided with 2-7 (preferably 3-5, such as 3,4,5,6 or 7) activated carbon chambers (such as a1, a2, a3, a4, a5, a6, a7; in this way) and located in the lower part in the flow direction of the flue gas (in this order) the thickness of these activated carbon chambers becomes thicker in turn or any two adjacent activated carbon chambers in the lower part (e.g. a2 and a3, or a3 and a 4) after the first activated carbon chamber in the lower part (a 1) in the flow direction of the flue gas, the thickness of the latter activated carbon chamber (e.g. a3 or a 4) being greater than or equal to the thickness of the former activated carbon chamber (e.g. a2 or e.g. a 3), the upper activated carbon bed part (B) having 2-7 (preferably 3-5, e.g. 3,4,5,6 or 7) activated carbon chambers (e.g. B1, B2, B3, B4, B5, B6, B7 when there are 7 in turn numbered; pushing in this way) and the thickness of these activated carbon chambers located in the upper part in the flow direction of the flue gas (in this order) becomes thicker in turn or the thickness (e.g. b3 or e.g. b 4) of the latter activated carbon chamber is greater than or equal to the thickness of the former activated carbon chamber (e.g. b2 or e.g. b 3) of any two adjacent activated carbon chambers in the upper part (e.g. b2 and b3, or b3 and b 4) behind the first activated carbon chamber in the upper part in the flow direction of the flue gas (b 1).
Preferably, the thickness of the second chamber (a 2 or b 2) is 1 to 9 times (e.g., 1.5 to 7 times, such as 2, 3,4,5 or 6 times) the thickness of the first chamber (a 1 or b 1) in the order of the flow direction of the flue gas, among the 2 to 7 (e.g., 3) activated carbon chambers located at the lower portion or among the 2 to 7 (e.g., 3) activated carbon chambers located at the upper portion. Furthermore, when there is a third chamber (a 3 or b 3), the thickness of the third chamber (a 3 or b 3) is 1-2.5 times (preferably 1.2-2 times, for example 1.3 times, 1.5 times, or 1.8 times) the thickness of the second chamber (a 2 or b 2). By adopting the structural design, the moving speed of the solid adsorption medium (or called solid medium, such as activated carbon or activated coke) of the front chamber is greater than or equal to the moving speed of the solid adsorption medium (or called solid medium) of the rear chamber.
Typically, the lower portion has 3 activated carbon chambers, the thickness of the first chamber (a 1) (i.e., the front chamber), the second chamber (a 2) (i.e., the middle chamber) and the third chamber (a 3) (i.e., the rear chamber) being 90-250mm (preferably 100-230mm, such as 120, 150, 200 or 220 mm), 360-1000mm (preferably 400-950mm, such as 450, 600, 700, 800 or 900 mm) and 432-1200mm (preferably 450-1150mm, such as 500, 600, 700, 800, 900, 1000 or 1100 mm), respectively, in the order of the flow direction of the flue gas.
Typically, the upper part has 3 activated carbon chambers, the thickness of the first chamber (b 1) (i.e. the front chamber), the second chamber (b 2) (i.e. the middle chamber) and the third chamber (b 3) (i.e. the rear chamber) being 90-250mm (preferably 100-230mm, such as 120, 150, 200 or 220 mm), 360-1000mm (preferably 400-950mm, such as 450, 600, 700, 800 or 900 mm) and 432-1200mm (preferably 450-1150mm, such as 500, 600, 700, 800, 900, 1000 or 1100 mm), respectively, in the order of the flow direction of the flue gas.
Preferably, the flue gas inlet (1) located at the lower part of the adsorption tower and the flue gas outlet (2) located at the upper part of the adsorption tower are located at the same side of the adsorption tower.
Preferably, there is a roll feeder (6) at the bottom of each chamber of the lower activated carbon bed section (a).
Preferably, one or more blowdown rotary valves (7) are provided in the bottom bin of the adsorption column.
Typically, there are a plurality (e.g., 2-7, such as 3,4,5, 6) activated carbon channels (10) in the transition zone (C). Preferably, these activated carbon channels (10) consist of a partition (9) and the tower wall of the adsorption tower, or of a circular cross-section cylinder (9) or cone (9), or of an oval cross-section tube or cylinder (9) or polygonal (e.g. triangular or rectangular or pentagonal or hexagonal) cross-section tube or cylinder (9). More preferably, the partition (9) or the cylinder (9) or the cone (9) is a perforated plate or a cylinder or cone made of a perforated plate. More preferably, the tube or cylinder (9) is a tube or cylinder made of a non-porous plate.
Preferably, the upper 2-7 (preferably 3-5, e.g. 3,4,5,6 or 7) activated carbon chambers communicate via respective activated carbon channels (10) to the corresponding lower 2-7 (preferably 3-5, e.g. 3,4,5,6 or 7) activated carbon chambers.
Preferably, at the middle position in the vertical direction of the transition zone (C), the sum of the cross-sectional areas of all the activated carbon channels (10) is less than or equal to the sum of the cross-sectional areas of all the activated carbon chambers in the upper part or the sum of the cross-sectional areas of all the activated carbon chambers in the lower part, preferably the former is 20% -60%, preferably 20-50%, more preferably 22-35% of the latter.
The height of the transition zone (C) of the adsorption column or the length of the transition zone (C) of the adsorption column in the vertical direction is 1 to 5m, preferably 1.2 to 4m, more preferably 1.5 to 3m.
Preferably, the bottom of each of the upper activated carbon chambers is equipped with a roll feeder (6), preferably, these roll feeders (6) are located in the transition zone (C) of the adsorption tower and these roll feeders (6) are kept at a gap or vertical distance from the activated carbon layer of each of the lower activated carbon chambers (i.e. the rolls of the roll feeders (6) are not in contact with the activated carbon layer of each of the lower activated carbon chambers).
In general, the height of the main structure of the adsorption column is 6 to 60m (meter), preferably 8 to 55m (meter), preferably 10 to 50m, preferably 15 to 45m,18 to 40m, preferably 20 to 35m, preferably 22 to 30m. The height of the main structure of the adsorption tower means the height from the inlet to the outlet of the adsorption tower (main structure).
The ratio of the packing height of the solid adsorption medium or solid adsorbent (e.g. activated carbon) in the lower activated carbon bed section (a) to the packing (filling) height of the solid adsorption medium or solid adsorbent (e.g. activated carbon) in the upper activated carbon bed section (B) is 3:1-1:3, preferably 2:1-1:2, preferably 1.8:1-1:1.8, more preferably 1.5:1-1:1.5, more preferably 1.2:1-1:1.2, such as 1:1.
In this application, activated carbon refers to activated carbon in a broad sense, which includes: conventional activated carbon, activated coke, carbon-based adsorption media, carbon-based catalysts, and the like. In addition, solid adsorbents or solid adsorption media can be substituted for the above-described broad-sense activated carbon, and shall fall within the scope of protection in the present application.
In addition, in the present application, the flue gas broadly includes: conventional industrial fumes or industrial waste gases.
By means of the structural design, the downward moving speed or the blanking speed or the active carbon residence time of each active carbon bed layer at the upper part and each active carbon bed layer at the lower part in the adsorption tower can be controlled independently or respectively. In addition, it is made possible to ensure that: in steady operation, the total amount of active carbon discharged in the upper active carbon bed layer and the lower active carbon bed layer in unit time is equal. Alternatively, it may be controlled by a roll feeder in the lower activated carbon bed section a only (i.e., bed a). Whichever way of blanking speed control is used, the moving speed of the solid medium in the front chamber is greater than or equal to that in the rear chamber.
According to a second embodiment of the present utility model, there is provided a flue gas cleaning method (or a desulfurization, denitration method of flue gas or sintering flue gas using the above apparatus) employing the above apparatus, the method comprising:
1) Flue gas or sintered flue gas (hereinafter, both are collectively referred to as flue gas) is fed to an activated carbon adsorption tower comprising one of the above-mentioned activated carbon adsorption tower and (conventional) desorption tower, flows through a lower activated carbon bed portion (a) and an upper activated carbon bed portion (B) in this order and comes into contact with activated carbon fed into these two portions (a) and (B) from the top of the adsorption tower, so that contaminants including sulfur oxides, nitrogen oxides and dioxins are adsorbed by the activated carbon;
2) Transferring the activated carbon having absorbed pollutants from flue gas or sintered flue gas in an activated carbon adsorption tower of a desulfurization and denitrification device from the bottom of the adsorption tower to a heating zone of an activated carbon desorption tower having an upper heating zone and a lower cooling zone, and heating or raising the temperature to an activated carbon desorption temperature Td (for example, td=390-450 ℃) by indirect heat exchange between the activated carbon and hot air as heating gas, so that the activated carbon is desorbed and regenerated at the temperature Td; and
3) The activated carbon which is resolved and regenerated in the heating area at the upper part of the resolving tower enters the cooling area at the lower part of the resolving tower through a middle buffer area, namely a middle section, and meanwhile, the normal-temperature air (as cooling air or cooling air) is introduced into the cooling area of the resolving tower from a cold air inlet of the cooling area of the resolving tower, and indirect heat exchange is carried out with the activated carbon which moves downwards in the cooling area to cool the activated carbon; and
4) The cooled activated carbon exiting the bottom of the resolving tower (e.g., after removal of ash by sieving) is transferred to the top (e.g., top feed bin) of the activated carbon adsorption tower of step (1) above.
Generally, the activated carbon regeneration temperature Td is in the range of 390-500 ℃, preferably 400-470 ℃, more preferably 405-450 ℃, more preferably 410-440 ℃, more preferably 410-430 ℃.
Generally, the hot air fed into the heating zone of the analytical column has a temperature of 400 to 500 ℃, preferably 410 to 480 ℃, more preferably 415 to 470 ℃, still more preferably 420 to 460 ℃, still more preferably 420 to 450 ℃.
In the above method, in the adsorption tower, the downward moving speed or the discharging speed or the active carbon residence time of each of the upper active carbon bed layer and the lower active carbon bed layer can be controlled individually or separately. In steady operation, the total amount of active carbon discharged in the upper active carbon bed layer and the lower active carbon bed layer in unit time is equal.
The analysis column of the present utility model is an analysis column or a regeneration column used in a dry desulfurization/denitration apparatus for treating an exhaust gas in the iron and steel industry, and generally has a column height of 10 to 45m, preferably 15 to 40m, more preferably 20 to 35 m. The desorber typically has a length of 6 to 100 meters 2 Preferably 8-50 meters 2 More preferably 10-30 meters 2 Further preferably 15-20 meters 2 Is a cross-sectional area of the body of the (c). Whereas the (desulfurization, denitrification) adsorption columns (or reaction columns) in the desulfurization and denitrification apparatus generally have a larger size, for example, the column height of the adsorption column is 6 to 60m (meters), preferably 8 to 55m (meters), preferably 10 to 50m, preferably 15 to 45m,18 to 40m, preferably 20 to 35m, preferably 22 to 30m. The column height of the adsorption column refers to the height from the activated carbon outlet at the bottom of the adsorption column to the activated carbon inlet at the top of the adsorption column, i.e., the height of the main structure of the column.
For the design of flue gas (or exhaust gas) adsorption towers and their adsorption processes, there have been many documents in the prior art, see for example US5932179, JP2004209332A, and JP3581090B2 (JP 2002095930 a) and JP3351658B2 (JPH 08332347 a), JP2005313035A. This application is not described in detail.
In the present utility model, there is no particular requirement for the resolution column, and the resolution column of the prior art can be used in the present utility model. Preferably, the column is a shell-and-tube type vertical column in which the activated carbon is fed from the top of the column, flows down through a tube pass, then reaches the bottom of the column, and the heated gas flows through the shell pass, and the heated gas enters from one side of the column, exchanges heat with the activated carbon flowing through the tube pass to cool, and then is fed out from the other side of the column. Preferably, the column is a shell-and-tube type (or shell-and-tube type) or column type vertical column in which the activated carbon is fed from the top of the column, flows downward through the tube side of the upper heating zone, then reaches a buffer space between the upper heating zone and the lower cooling zone, then flows through the tube side of the lower cooling zone, then reaches the bottom of the column, and the heated gas (or high-temperature hot air) flows through the shell side of the heating zone, and the heated gas (400-500 ℃) enters from one side of the heating zone of the column, undergoes indirect heat exchange with the activated carbon flowing through the tube side of the heating zone to be cooled, and then is fed from the other side of the heating zone of the column. The cooling air enters from one side of the cooling zone of the desorption tower and carries out indirect heat exchange with the desorbed and regenerated active carbon flowing through the tube side of the cooling zone. After indirect heat exchange, the cooling air is warmed to 120±20 ℃, e.g., about 120 ℃.
As for the design of the activated carbon desorption column and the method of regenerating activated carbon, many documents have been disclosed in the prior art, and JP3217627B2 (JPH 08155299 a) discloses a desorption column (i.e., a desorption column) which adopts a double seal valve, seals with inert gas, sieves, and water-cools (see fig. 3 of the patent). JP3485453B2 (JPH 11104457A) discloses a regeneration column (see FIGS. 23 and 24 of the patent) which may employ a preheating stage, double seal valves, inert gas feed, air cooling or water cooling. JPS59142824a discloses gas from a cooling section for preheating activated carbon. Chinese patent application 201210050541.6 (shanghai sulfur corporation) discloses a scheme for energy reuse of a regeneration tower, in which a dryer 2 is used. JPS4918355B discloses the use of blast furnace gas (blast furnace gas) to regenerate activated carbon. JPH08323144a discloses a regenerator using fuel (heavy oil or light oil) using an air heating furnace (see fig. 2, 11-hot blast stove, 12-fuel supply device of that patent). Chinese utility model 201320075942.7 relates to a heating device and an exhaust gas treatment device (coal-fired, air-heated) equipped with the heating device, and is shown in fig. 2 of the patent.
The analytical tower of the utility model adopts air cooling.
In the case of an analytical tower with an analytical capacity of 10t of activated carbon per hour, the conventional process requires about 400Nm of coke oven gas to maintain the temperature in the analytical tower at 420 deg.C 3 /h, combustion air of about 2200Nm 3 And/h, the external heat exhaust air is about 2500Nm 3 /h; required cooling air 30000Nm 3 And/h, the temperature of the cooled activated carbon is 140 ℃.
In this application "optional" means with or without, "optionally" means with or without. The resolving tower and the regenerating tower can be used interchangeably. Regeneration and resolution are used interchangeably. In addition, the analysis and desorption are the same concept. The "heating section" is the same concept as the "heating zone". The "cooling section" is the same concept as the "cooling zone".
The thickness of the activated carbon chamber refers to the distance or spacing between the two porous partitions of the activated carbon chamber.
Advantages or advantageous technical effects of the utility model
1. The adsorption tower equipment of the utility model obviously improves the flue gas treatment capacity, reduces the equipment manufacturing, running and maintaining costs and saves electric energy and heat energy.
2. The process is easier to control, and dead angles of air flow are avoided.
3. The equipment is compact and convenient to maintain.
4. The residence time of the activated carbon in each part in the adsorption tower is very matched with the adsorption capacity of the activated carbon, and the utilization rate of the activated carbon is high.
5. The primary filling amount of the activated carbon is reduced, the investment cost is reduced, and the residence time of the activated carbon which is not contacted with the flue gas in the tower is reduced.
Drawings
FIG. 1 is a schematic diagram of a prior art desulfurization and denitrification device including an activated carbon adsorption tower and an activated carbon regeneration tower and a process flow.
Fig. 2 is a schematic diagram of an adsorption column of the prior art.
Fig. 3 is a schematic diagram of another adsorption column of the prior art.
Fig. 4,5 and 6 are schematic views of three adsorption towers of the present utility model.
Reference numerals:
A. the active carbon bed layer part at the lower part, the active carbon bed layer part at the upper part, the transition zone at the middle part of the adsorption tower, 1, a smoke inlet, 2, a smoke outlet, 3, a feeding bin, 4, a porous partition board, 4', a porous partition board or shutter, 5, a smoke channel, 6, a roller feeder, 7, a rotary valve, 8, a conveying device, 9, a non-porous partition board or a cylinder or cone made of a non-porous plate, and 10, the active carbon channel in the transition zone (C).
a1, a first active carbon chamber at the lower part, a2, a second active carbon chamber at the lower part, a3, a third active carbon chamber at the lower part, b1, a first active carbon chamber at the upper part, b2, a second active carbon chamber at the upper part, b3 and a third active carbon chamber at the upper part.
G1, the flue gas inlet end of the lower activated carbon bed part (a), G2, the flue gas outlet end of the lower activated carbon bed part (a), G3, the flue gas inlet end of the upper activated carbon bed part (B), G4, the flue gas outlet end of the upper activated carbon bed part (B).
Detailed Description
The desulfurization and denitrification apparatus used in the examples includes an activated carbon adsorption tower and a desorption tower. The activated carbon desorber has an upper heating zone and a lower cooling zone and an intermediate buffer zone therebetween.
The sintering flue gas to be treated in the examples is sintering machine flue gas from the steel industry.
In an embodiment, the size of the analytical column is: the tower height is 20m, and the main body cross section area is 15m 2 。
The structure of the three adsorption towers is shown in fig. 4-6.
An activated carbon process gas cleaning apparatus comprising an activated carbon adsorption column (i.e., a desulfurization and denitrification apparatus comprising an activated carbon adsorption column and a desorption column or an activated carbon process gas cleaning apparatus comprising an activated carbon adsorption column and a desorption column) comprising a lower activated carbon bed portion (A), an upper activated carbon bed portion (B) and a transition zone (C) (or referred to as an intermediate zone (C)) between the two portions, and the activated carbon adsorption tower comprises a feeding bin (3) positioned above or at the top of the adsorption tower, a flue gas inlet (1) positioned at the lower part of the adsorption tower and a flue gas outlet (2) positioned at the upper part of the adsorption tower, wherein a flue gas outflow end (G2) of the lower activated carbon bed part (A) is communicated with a flue gas inlet end (G3) of the upper activated carbon bed part (B) through a flue gas channel (5), the lower activated carbon bed part (A) is provided with 2-7 (preferably 3-5, such as 3,4,5,6 or 7) activated carbon chambers (such as a1, a2, a3, a4, a5, a6, a7; in this way) and located in the lower part in the flow direction of the flue gas (in this order) the thickness of these activated carbon chambers becomes thicker in turn or any two adjacent activated carbon chambers in the lower part (e.g. a2 and a3, or a3 and a 4) after the first activated carbon chamber in the lower part (a 1) in the flow direction of the flue gas, the thickness of the latter activated carbon chamber (e.g. a3 or a 4) being greater than or equal to the thickness of the former activated carbon chamber (e.g. a2 or e.g. a 3), the upper activated carbon bed part (B) having 2-7 (preferably 3-5, e.g. 3,4,5,6 or 7) activated carbon chambers (e.g. B1, B2, B3, B4, B5, B6, B7 when there are 7 in turn numbered; pushing in this way) and the thickness of these activated carbon chambers located in the upper part in the flow direction of the flue gas (in this order) becomes thicker in turn or the thickness (e.g. b3 or e.g. b 4) of the latter activated carbon chamber is greater than or equal to the thickness of the former activated carbon chamber (e.g. b2 or e.g. b 3) of any two adjacent activated carbon chambers in the upper part (e.g. b2 and b3, or b3 and b 4) behind the first activated carbon chamber in the upper part in the flow direction of the flue gas (b 1).
Preferably, the thickness of the second chamber (a 2 or b 2) is 1 to 9 times (e.g., 1.5 to 7 times, such as 2, 3,4,5 or 6 times) the thickness of the first chamber (a 1 or b 1) in the order of the flow direction of the flue gas, among the 2 to 7 (e.g., 3) activated carbon chambers located at the lower portion or among the 2 to 7 (e.g., 3) activated carbon chambers located at the upper portion. Furthermore, when there is a third chamber (a 3 or b 3), the thickness of the third chamber (a 3 or b 3) is 1-2.5 times (preferably 1.2-2 times, for example 1.3 times, 1.5 times, or 1.8 times) the thickness of the second chamber (a 2 or b 2).
Typically, the lower portion has 3 activated carbon chambers, the thickness of the first chamber (a 1) (i.e., the front chamber), the second chamber (a 2) (i.e., the middle chamber) and the third chamber (a 3) (i.e., the rear chamber) being 90-250mm (preferably 100-230mm, such as 120, 150, 200 or 220 mm), 360-1000mm (preferably 400-950mm, such as 450, 600, 700, 800 or 900 mm) and 432-1200mm (preferably 450-1150mm, such as 500, 600, 700, 800, 900, 1000 or 1100 mm), respectively, in the order of the flow direction of the flue gas.
Typically, the upper part has 3 activated carbon chambers, the thickness of the first chamber (b 1) (i.e. the front chamber), the second chamber (b 2) (i.e. the middle chamber) and the third chamber (b 3) (i.e. the rear chamber) being 90-250mm (preferably 100-230mm, such as 120, 150, 200 or 220 mm), 360-1000mm (preferably 400-950mm, such as 450, 600, 700, 800 or 900 mm) and 432-1200mm (preferably 450-1150mm, such as 500, 600, 700, 800, 900, 1000 or 1100 mm), respectively, in the order of the flow direction of the flue gas.
Preferably, the flue gas inlet (1) located at the lower part of the adsorption tower and the flue gas outlet (2) located at the upper part of the adsorption tower are located at the same side of the adsorption tower.
Preferably, there is a roll feeder (6) at the bottom of each chamber of the lower activated carbon bed section (a).
Preferably, one or more blowdown rotary valves (7) are provided in the bottom bin of the adsorption column.
Typically, there are a plurality (e.g., 2-7, such as 3,4,5, 6) activated carbon channels (10) in the transition zone (C). Preferably, these activated carbon channels (10) consist of a partition (9) and the tower wall of the adsorption tower, or of a circular cross-section cylinder (9) or cone (9), or of an oval cross-section tube or cylinder (9) or polygonal (e.g. triangular or rectangular or pentagonal or hexagonal) cross-section tube or cylinder (9). More preferably, the partition (9) or the cylinder (9) or the cone (9) is a perforated plate or a cylinder or cone made of a perforated plate. More preferably, the tube or cylinder (9) is a tube or cylinder made of a non-porous plate.
Preferably, the upper 2-7 (preferably 3-5, e.g. 3,4,5,6 or 7) activated carbon chambers communicate via respective activated carbon channels (10) to the corresponding lower 2-7 (preferably 3-5, e.g. 3,4,5,6 or 7) activated carbon chambers.
Preferably, at the middle position in the vertical direction of the transition zone (C), the sum of the cross-sectional areas of all the activated carbon channels (10) is smaller than or equal to the sum of the cross-sectional areas of all the activated carbon chambers in the upper part or the sum of the cross-sectional areas of all the activated carbon chambers in the lower part, preferably the former is 20% -60%, preferably 20% -50% of the latter.
The height of the transition zone (C) of the adsorption column or the length of the transition zone (C) of the adsorption column in the vertical direction is 1 to 5m, preferably 1.2 to 4m, more preferably 1.5 to 3m.
Preferably, the bottom of each of the upper activated carbon chambers is equipped with a roll feeder (6), preferably, these roll feeders (6) are located in the transition zone (C) of the adsorption tower and these roll feeders (6) are kept at a gap or vertical distance from the activated carbon layer of each of the lower activated carbon chambers (i.e. the rolls of the roll feeders (6) are not in contact with the activated carbon layer of each of the lower activated carbon chambers).
In general, the height of the main structure of the adsorption column is 6 to 60m (meter), preferably 8 to 55m (meter), preferably 10 to 50m, preferably 15 to 45m,18 to 40m, preferably 20 to 35m, preferably 22 to 30m.
According to a second embodiment of the present utility model, there is provided a flue gas cleaning (or sintering flue gas desulfurization, denitration method) using the above apparatus, the method comprising:
1) The flue gas (containing pollutants) or the sintering flue gas (hereinafter, both are collectively referred to as flue gas) is fed to an activated carbon adsorption column comprising one of the above-mentioned activated carbon adsorption column and (conventional) desorption column, flows through the lower activated carbon bed portion (a) and the upper activated carbon bed portion (B) in this order and comes into contact with the activated carbon fed into these two portions (a) and (B) from the top of the adsorption column, so that the pollutants including sulfur oxides, nitrogen oxides and dioxins are adsorbed by the activated carbon;
2) Transferring the activated carbon having absorbed pollutants from flue gas or sintered flue gas in an activated carbon adsorption tower of a desulfurization and denitrification device from the bottom of the adsorption tower to a heating zone of an activated carbon desorption tower having an upper heating zone and a lower cooling zone, and heating or raising the temperature to an activated carbon desorption temperature Td (for example, td=390-450 ℃) by indirect heat exchange between the activated carbon and hot air as heating gas, so that the activated carbon is desorbed and regenerated at the temperature Td; and
3) The activated carbon which is resolved and regenerated in the heating area at the upper part of the resolving tower enters the cooling area at the lower part of the resolving tower through a middle buffer area, namely a middle section, and meanwhile, the normal-temperature air (as cooling air or cooling air) is introduced into the cooling area of the resolving tower from a cold air inlet of the cooling area of the resolving tower, and indirect heat exchange is carried out with the activated carbon which moves downwards in the cooling area to cool the activated carbon; and
4) The cooled activated carbon exiting the bottom of the resolving tower (e.g., after removal of ash by sieving) is transferred to the top (e.g., top feed bin) of the activated carbon adsorption tower of step (1) above.
Generally, the activated carbon regeneration temperature Td is in the range of 390-500 ℃, preferably 400-470 ℃, more preferably 405-450 ℃, more preferably 410-440 ℃, more preferably 410-430 ℃.
Generally, the hot air fed into the heating zone of the analytical column has a temperature of 400 to 500 ℃, preferably 410 to 480 ℃, more preferably 415 to 470 ℃, still more preferably 420 to 460 ℃, still more preferably 420 to 450 ℃.
Example 1
The adsorption tower is shown in fig. 4. The desulfurization and denitrification device comprises an activated carbon adsorption tower (tower height is 30m, cross-sectional area is 120 m) 2 ) And a resolving tower (tower height 20m, cross-sectional area 15 m) 2 )。
The lower activated carbon bed section a has three activated carbon chambers a1, a2 and a3 and the upper activated carbon bed section B has three activated carbon chambers B1, B2 and B3.
Along the air flow direction, defining each layer as a lower layer front chamber, a middle chamber and a rear chamber according to the front-rear sequence of each layer of activated carbon contacting with the flue gas; upper front, middle and rear chambers. The thicknesses of the front, middle and rear chambers of the lower layer are respectively 150mm, 450mm and 900mm, and the total thickness is 1500mm; the thicknesses of the front, middle and rear chambers of the upper layer are respectively 150mm, 450mm and 900mm, and the total thickness is 1500mm; thereby controlling the residence time of the active carbon in the front, middle and rear chambers of the upper and lower layers to be 40h, 120h and 240h, for example.
The upper and lower discharging can be adjusted.
The device of the embodiment divides the adsorption tower into an upper layer and a lower layer, each layer of activated carbon is divided into multiple chambers by adopting a porous partition plate, and the flow speed (or the residence time) of the activated carbon in each chamber is respectively controlled by adopting a roller feeder below each chamber.
The activated carbon chamber a1 or b1 which is preferentially contacted with the flue gas is thinner, and the activated carbon which is saturated in adsorption is discharged as soon as possible by adopting a faster discharging speed; the active carbon chamber in each layer which is finally contacted with the flue gas is thicker, the residence time of the active carbon in the chamber is longer, and the dust concentration in the flue gas can be effectively reduced.
At the middle position in the vertical direction of the transition zone C, the sum of the cross-sectional areas of all the activated carbon channels 10 is about 55% of the sum of the cross-sectional areas of all the activated carbon chambers in the upper part or the sum of the cross-sectional areas of all the activated carbon chambers in the lower part. The height of the transition zone (C) of the adsorption column or the length of the transition zone (C) of the adsorption column in the vertical direction is 2m.
The upper activated carbon is discharged by a roller feeder and then is placed at the top of the lower activated carbon chamber for temporary storage.
The lower part of the roller feeder is not contacted with the activated carbon, so that the roller and the activated carbon are prevented from being rubbed to generate high temperature or spark.
Example 2
The adsorption tower is shown in fig. 5. For the flue gas with little fluctuation of pollutant components, a roller feeder for feeding the upper layer can be omitted, and the residence time of materials in each layer is realized by controlling the width of each chamber of the upper layer and the lower layer. The height of the transition zone (C) of the adsorption column or the length of the transition zone (C) of the adsorption column in the vertical direction is 3m.
Along the air flow direction, defining each layer as a lower layer front chamber, a middle chamber and a rear chamber according to the front-rear sequence of each layer of activated carbon contacting with the flue gas; upper front, middle and rear chambers. The thicknesses of the front, middle and rear chambers of the lower layer are respectively 150mm, 450mm and 900mm, and the total thickness is 1500mm; the thicknesses of the front, middle and rear chambers of the upper layer are respectively 150mm, 450mm and 900mm, and the total thickness is 1500mm; thereby controlling the residence time of the active carbon in the front, middle and rear chambers of the upper and lower layers to be 40h, 120h and 240h, for example.
Example 3
The adsorption tower is shown in fig. 6. In order to reduce the initial filling amount of the activated carbon, reduce investment cost, and reduce the residence time of the activated carbon which is not contacted with the flue gas in the tower, the length of an activated carbon channel between the upper layer and the lower layer can be shortened.
Along the air flow direction, defining each layer as a lower layer front chamber, a middle chamber and a rear chamber according to the front-rear sequence of each layer of activated carbon contacting with the flue gas; upper front, middle and rear chambers. The thicknesses of the front, middle and rear chambers of the lower layer are respectively 150mm, 450mm and 900mm, and the total thickness is 1500mm; the thicknesses of the front, middle and rear chambers of the upper layer are respectively 150mm, 450mm and 900mm, and the total thickness is 1500mm; thereby controlling the residence time of the active carbon in the front, middle and rear chambers of the upper and lower layers to be 40h, 120h and 240h, for example.
The intermediate activated carbon channels 10 are of ineffective area, so that the height (or length) and total cross-sectional area of the activated carbon channels (activated carbon channels) are reduced as much as possible while ensuring a low activated carbon discharge rate (low resistance). At the middle position in the vertical direction of the transition zone C, the sum of the cross-sectional areas of all the activated carbon channels 10 is 22% of the sum of the cross-sectional areas of all the activated carbon chambers in the upper part or the sum of the cross-sectional areas of all the activated carbon chambers in the lower part. The height of the transition zone (C) of the adsorption column or the length of the transition zone (C) of the adsorption column in the vertical direction is 1.8m.

Claims (19)

1. Including an active carbon adsorption tower's an active carbon method fume purification device, its characterized in that: the activated carbon adsorption tower comprises a lower activated carbon bed part (A), an upper activated carbon bed part (B) and a transition zone (C) between the two parts, and the activated carbon adsorption tower comprises a feeding bin (3) positioned above or at the top of the adsorption tower, a flue gas inlet (1) positioned at the lower part of the adsorption tower and a flue gas outlet (2) positioned at the upper part of the adsorption tower, wherein a flue gas outflow end (G2) of the lower activated carbon bed part (A) is communicated with a flue gas inlet end (G3) of the upper activated carbon bed part (B) through a flue gas channel (5), the lower activated carbon bed part (A) is provided with 2-7 activated carbon chambers separated by a porous partition plate (4) and the thickness of the activated carbon chambers positioned at the lower part sequentially thickens along the flow direction of flue gas, and the upper activated carbon bed part (B) is provided with 2-7 activated carbon chambers separated by the porous partition plate (4) and the thickness of the activated carbon chambers positioned at the upper part sequentially thickens along the flow direction of the flue gas;
wherein in the transition zone (C) there are a plurality of activated carbon channels (10); the activated carbon channels (10) are formed by a partition plate (9) and the tower wall of the adsorption tower, or are formed by a cylinder or a cone with a circular cross section, or are formed by a tube or a cylinder with an elliptical cross section or a tube or a cylinder with a polygonal cross section; wherein the upper 2-7 activated carbon chambers are communicated to the lower corresponding 2-7 activated carbon chambers via respective activated carbon channels (10); wherein the bottom of each of the upper activated carbon chambers is provided with roll feeders (6), which roll feeders (6) are located in the transition zone (C) of the adsorption tower and which roll feeders (6) are kept with a gap or a vertical distance from the activated carbon layer of each of the lower activated carbon chambers, i.e. the rolls of the roll feeders (6) are not in contact with the activated carbon layer of each of the lower activated carbon chambers.
2. The purification apparatus of claim 1, wherein: the lower activated carbon bed part (A) is provided with 3-5 activated carbon chambers separated by a porous baffle plate (4); the upper activated carbon bed section (B) has 3-5 activated carbon chambers separated by porous partition plates (4).
3. The purification device according to claim 1 or 2, characterized in that: wherein the thickness of the lower second chamber (a 2) or the upper second chamber (b 2) among the 2-7 activated carbon chambers located at the lower part or among the 2-7 activated carbon chambers located at the upper part is 1.5-7 times the thickness of the lower first chamber (a 1) or the upper first chamber (b 1), respectively, in the order of the flow direction of the flue gas, and when there is the lower third chamber (a 3) or the upper third chamber (b 3), the thickness of the lower third chamber (a 3) or the upper third chamber (b 3) is 1.2-2 times the thickness of the lower second chamber (a 2) or the upper second chamber (b 2), respectively.
4. A purification apparatus according to claim 3, wherein: the thickness of the lower second chamber (a 2) or the upper second chamber (b 2) is 2 or 3 times the thickness of the lower first chamber (a 1) or the upper first chamber (b 1), respectively, and when there is a lower third chamber (a 3) or an upper third chamber (b 3), the thickness of the lower third chamber (a 3) or the upper third chamber (b 3) is 1.3 times, 1.5 times or 1.8 times the thickness of the lower second chamber (a 2) or the upper second chamber (b 2), respectively.
5. A purification apparatus according to claim 3, wherein: wherein the lower part is provided with 3 active carbon chambers, and the thicknesses of the lower first chamber (a 1), the lower second chamber (a 2) and the lower third chamber (a 3) are respectively 90-250mm, 360-1000mm and 432-1200mm according to the flowing direction of the flue gas; and/or
The upper part is provided with 3 active carbon chambers, and the thicknesses of the upper first chamber (b 1), the upper second chamber (b 2) and the upper third chamber (b 3) are respectively 90-250mm, 360-1000mm and 432-1200mm according to the flowing direction of the flue gas.
6. The purification apparatus of claim 5, wherein: the thickness of the lower first chamber (a 1), the lower second chamber (a 2) and the lower third chamber (a 3) is 100-230mm, 400-950mm and 450-1150mm, respectively; and/or
The thickness of the upper first chamber (b 1), the upper second chamber (b 2) and the upper third chamber (b 3) is 100-230mm, 400-950mm and 450-1150mm, respectively.
7. The purification apparatus of claim 6, wherein: the lower first chamber (a 1) has a thickness of one of 120mm, 150mm, 200mm or 220 mm; the lower second chamber (a 2) has a thickness of one of 450mm, 600mm, 700mm, 800mm or 900 mm; the lower third chamber (a 3) has a thickness of one of 500mm, 600mm, 700mm, 800mm, 900mm, 1000mm or 1100 mm; and/or
The upper first chamber (b 1) has a thickness of one of 120mm, 150mm, 200mm or 220 mm; the upper second chamber (b 2) has a thickness of one of 450mm, 600mm, 700mm, 800mm or 900 mm; the thickness of the upper third chamber (b 3) is one of 500mm, 600mm, 700mm, 800mm, 900mm, 1000mm or 1100 mm.
8. The purification apparatus of any one of claims 1-2, 4-7, wherein: wherein the flue gas inlet (1) positioned at the lower part of the adsorption tower and the flue gas outlet (2) positioned at the upper part of the adsorption tower are positioned at the same side of the adsorption tower.
9. A purification apparatus according to claim 3, wherein: wherein the flue gas inlet (1) positioned at the lower part of the adsorption tower and the flue gas outlet (2) positioned at the upper part of the adsorption tower are positioned at the same side of the adsorption tower.
10. The purification apparatus of any one of claims 1-2, 4-7, 9, wherein: wherein a roller feeder (6) is provided at the bottom of each chamber of the lower activated carbon bed section (A); and/or
The bottom bin of the adsorption tower is provided with one or more discharging rotary valves (7).
11. A purification apparatus according to claim 3, wherein: wherein a roller feeder (6) is provided at the bottom of each chamber of the lower activated carbon bed section (A); and/or
The bottom bin of the adsorption tower is provided with one or more discharging rotary valves (7).
12. The purification apparatus of claim 1, wherein: the partition (9) or the cylinder or the cone is a non-porous plate or a cylinder or a cone made of a non-porous plate, and the tube or the cylinder is a tube or a cylinder made of a non-porous plate.
13. The purification apparatus of claim 12, wherein: the number of the upper activated carbon chambers is 3-5, which are connected to the corresponding lower activated carbon chambers via respective activated carbon channels (10).
14. The purification apparatus of any one of claims 1-2, 4-7, 9, 11-13, wherein: wherein the sum of the cross-sectional areas of all the activated carbon channels (10) is smaller than or equal to the sum of the cross-sectional areas of all the activated carbon chambers in the upper part or the sum of the cross-sectional areas of all the activated carbon chambers in the lower part at the middle position in the vertical direction of the transition zone (C).
15. A purification apparatus according to claim 3, wherein: wherein the sum of the cross-sectional areas of all the activated carbon channels (10) is smaller than or equal to the sum of the cross-sectional areas of all the activated carbon chambers in the upper part or the sum of the cross-sectional areas of all the activated carbon chambers in the lower part at the middle position in the vertical direction of the transition zone (C).
16. The purification apparatus of claim 14, wherein: the sum of the cross-sectional areas of all the activated carbon channels (10) is 20% -60% of the sum of the cross-sectional areas of all the activated carbon chambers in the upper part or the sum of the cross-sectional areas of all the activated carbon chambers in the lower part.
17. The purification apparatus of claim 15, wherein: the sum of the cross-sectional areas of all the activated carbon channels (10) is 20% -60% of the sum of the cross-sectional areas of all the activated carbon chambers in the upper part or the sum of the cross-sectional areas of all the activated carbon chambers in the lower part.
18. A method of purifying flue gas using the apparatus according to any one of claims 1 to 17, characterized in that: the method comprises the following steps:
1) A flue gas or a sintered flue gas is fed into a purification apparatus comprising any one of claims 1 to 17, which flue gas flows through the lower activated carbon bed section (a) and the upper activated carbon bed section (B) in this order and is contacted with activated carbon fed into these two sections (a) and (B) from the top of the adsorption tower, so that contaminants including sulfur oxides, nitrogen oxides and dioxins are adsorbed by the activated carbon;
2) Transferring the activated carbon, which has absorbed pollutants from flue gas or sintered flue gas in an activated carbon adsorption tower of a desulfurization and denitrification device, from the bottom of the adsorption tower to a heating zone of an activated carbon analysis tower having an upper heating zone and a lower cooling zone, and heating or raising the temperature to an activated carbon analysis temperature Td by indirect heat exchange between the activated carbon and hot air as heating gas, so that the activated carbon is analyzed and regenerated at the Td temperature; and
3) The activated carbon which is resolved and regenerated in the heating zone at the upper part of the resolving tower enters the cooling zone at the lower part of the resolving tower through a middle buffer zone, namely a middle section, and meanwhile, the cooling fan is used for introducing normal-temperature air into the cooling zone of the resolving tower from a cold air inlet of the cooling zone of the resolving tower, and indirect heat exchange is carried out with the activated carbon which moves downwards in the cooling zone to cool the activated carbon; and
4) The cooled activated carbon discharged from the bottom of the resolving tower is transferred into the top of the activated carbon adsorption tower of the above step 1).
19. The method according to claim 18, wherein: in step 2), td=390-450 ℃; in step 4), the cooled activated carbon is screened to remove ash and then transferred to the top feed bin of the activated carbon adsorption column of step 1) above.
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