CN106693603A - Activated carbon method flue gas cleaning device and flue gas cleaning method - Google Patents

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

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Publication number
CN106693603A
CN106693603A CN201510780033.7A CN201510780033A CN106693603A CN 106693603 A CN106693603 A CN 106693603A CN 201510780033 A CN201510780033 A CN 201510780033A CN 106693603 A CN106693603 A CN 106693603A
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activated carbon
chamber
flue gas
tower
adsorption tower
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CN201510780033.7A
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CN106693603B (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 MYPI2018701431A priority patent/MY192747A/en
Priority to RU2018117492A priority patent/RU2697688C1/en
Priority to BR112018009430-7A priority patent/BR112018009430B1/en
Publication of CN106693603A publication Critical patent/CN106693603A/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

Abstract

The invention discloses an activated carbon method flue gas cleaning device and a flue gas cleaning method. The device comprises an activated carbon adsorption tower, wherein the activated carbon adsorption tower comprises an activated carbon bed part (A), an activated carbon bed part (B), and a transition area (C) positioned between the two parts; the activated carbon adsorption tower comprises a feed bin (3), a flue gas inlet (1) and a flue gas outlet (2); the feed bin (3) is positioned above the adsorption tower; the flue gas inlet (1) is positioned on the lower part of the adsorption tower; the flue gas outlet (2) is positioned on the upper part of the adsorption tower; a flue gas outflow end (G2) of the activated carbon bed part (A) is communicated with a flue gas inflow end (G3) of the activated carbon bed part (B) through a flue gas channel (5); the activated carbon bed part (A) comprises 2-7 activated carbon chambers which are isolated by porous separators (4), and the thicknesses of the activated carbon chambers positioned on the lower part are sequentially increased along the flow direction of the flue gas; the activated carbon bed part (B) comprises 2-7 activated carbon chambers which are isolated by the porous separators (4), and the thicknesses of the activated carbon chambers positioned on the upper part are sequentially increased along the flow direction of the flue gas.

Description

Activated carbon method smoke eliminator and flue gas purifying method
Technical field
The present invention relates to activated carbon method smoke eliminator and flue gas purifying method, the device belongs to one kind and is controlled suitable for atmosphere pollution The activated carbon method smoke eliminator of reason, is related to field of environment protection.
Background technology
For industrial smoke, the especially sintering device flue gas of steel and iron industry, using de- including activated carbon adsorber and Analytic Tower Sulphur, denitrification apparatus and technique are more satisfactory.In the desulphurization and denitration including activated carbon adsorber and Analytic Tower (or regenerator) In device, activated carbon adsorber is used to include from sintering flue gas or waste gas (the especially sintering flue gas of the sintering machine of steel and iron industry) absorption Oxysulfide, nitrogen oxides and dioxin are in interior pollutant, and Analytic Tower is used for the hot recycling of activated carbon.
Activated carbon desulfurization have desulfurization degree it is high, can be while realizing denitration, Tuo bioxin, dedusting, not producing waste water and dregs etc. excellent Point, is extremely promising flue gas purifying method.Activated carbon can regenerate at high temperature, and when temperature is higher than 350 DEG C, absorption exists (sulfur dioxide is resolved, nitrogen for the pollutants such as oxysulfide, nitrogen oxides, dioxin on activated carbon generation fast resolving or decomposition Oxide is He bioxin is decomposed).And with the rising of temperature, the reproduction speed of activated carbon further speeds up, recovery time contracting Short, regenerating active carbon temperature is approximately equal to 430 DEG C preferably in general control Analytic Tower, therefore, preferable resolution temperature (or again Raw temperature) it is for example in 390-450 DEG C of scope, more preferably in 400-440 DEG C of scope.
Traditional active carbon desulfurization technique is as shown in fig. 1.Flue gas introduces adsorption tower by booster fan, and ammonia is sprayed into tower mouthful is entered With the mixed gas of air, to improve NOXRemoval efficiency, flue gas after purification enters the main smoke stack emission of sintering.Activated carbon by Tower top is added in adsorption tower, and is moved down in the presence of gravity and bottom of towe drawing mechanism.Analytic Tower activated carbon out by 2# activated carbon conveyers are delivered to adsorption tower, and the activated carbon after adsorption tower absorption pollutant saturation is discharged by bottom, the activity of discharge Charcoal is delivered to Analytic Tower by 1# activated carbon conveyers, carries out regenerating active carbon.
The effect of Analytic Tower is by the SO of charcoal absorption2Discharge, while temperature and certain stop more than 400 DEG C , bioxin decomposable asymmetric choice net more than 80% under time, activated carbon is recycled again after cooling, screening.The SO for discharging2Can make Sulfuric acid etc., the communicated device of activated carbon after parsing is sent to adsorption tower and is re-used to adsorb SO2And NOXDeng.
The NO in adsorption tower and Analytic TowerXThere is the reaction such as SCR, SNCR with ammonia, so as to remove NOX.Dust is by inhaling It is tightly held by activated carbon during attached tower, is separated in the vibratory sieve of Analytic Tower bottom, sends to ash silo for active carbon powder under sieve, then Blast furnace can be sent to or sintering is used as fuel.
Gas cleaning is carried out using activated carbon method, in order to improve clean-up effect, flue gas can be made to pass through multilayer active carbon bed.Multilayer Active carbon bed arrangement is broadly divided into up-down structure and front-end geometry, as shown in Figure 2.Active carbon bed is one overall in tower, Activated carbon is uniformly moved down using gravity.Along the flow direction of flue gas, first with the charcoal absorption of smoke contacts in flue gas more Multi-pollutant, discharges together with later active charcoal, the unadsorbed saturation of later active charcoal can be caused just to discharge in tower or above active Gas cleaning effect is not played in charcoal adsorption saturation still in tower.
Prior art takes the adsorption tower of tandem structure, as shown in Figure 3, but need to increase a set of activated carbon conveying device, Investment and operating cost are not only increased, also increases extras maintenance workload.
Therefore, for investment reduction and operating cost and raising clean-up effect, need to be using more reasonably active carbon purifying device.
The content of the invention
It is an object of the invention to provide a kind of activated carbon method smoke eliminator including activated carbon adsorber, the charcoal absorption Tower includes active-carbon bed layer segment (A), the active-carbon bed layer segment (B) on top and the transition between the two parts of bottom Area (C), and the activated carbon adsorber includes feeding warehouse (3), the bottom positioned at adsorption tower positioned at the top of adsorption tower or top Smoke inlet (1) and the exhanst gas outlet (2) positioned at the top of adsorption tower, the flue gas stream of the active-carbon bed layer segment (A) of its middle and lower part Go out end (G2) to be connected by exhaust gases passes (5) with the flue gas upstream end (G3) of the active-carbon bed layer segment (B) on top, the work of bottom Property charcoal bed part (A) there is 2-7 (preferably 3-5) the activated carbon chamber, the activated carbon on top isolated by porous barrier (4) Bed part (B) has 2-7 (preferably 3-5) the activated carbon chamber isolated by porous barrier (4).
It is preferred that, (that is, inhaled including activated carbon the invention provides a kind of activated carbon method smoke eliminator including activated carbon adsorber A kind of desulphurization and denitration device or a kind of activated carbon method gas cleaning including activated carbon adsorber and Analytic Tower of attached tower and Analytic Tower Device), the active-carbon bed layer segment (A) of the activated carbon adsorber including bottom, the active-carbon bed layer segment (B) on top and positioned at this Transition region (C) (or making mesozone (C)) between two parts, and the activated carbon adsorber includes being located at the top of adsorption tower Or the feeding warehouse (3) at top, the smoke inlet (1) positioned at the bottom of adsorption tower and the exhanst gas outlet (2) positioned at the top of adsorption tower, The flue gas upstream end of the flue gas outflow end (G2) of the active-carbon bed layer segment (A) of its middle and lower part and the active-carbon bed layer segment (B) on top (G3) be connected by exhaust gases passes (5), the active-carbon bed layer segment (A) of bottom have by porous barrier (4) isolation (or isolation and Into) 2-7 (preferably 3-5, such as 3,4,5,6 or 7) activated carbon chamber (such as when there is 7, compile successively Number be a1, a2, a3, a4, a5, a6, a7；Flow direction (according to this sequentially) by that analogy) and along flue gas is located at The thickness of these activated carbon chambers of bottom is thickening successively or flow direction along flue gas bottom first activated carbon chamber (a1) latter activated carbon chamber in the middle of the adjacent activated carbon chamber (such as a2 and a3, or a3 and a4) of bottom any two after The thickness of room (such as a3 or such as a4) is more than or equal to the thickness of previous activated carbon chamber (such as a2 or such as a3), top Active-carbon bed layer segment (B) have by porous barrier (4) isolation (or isolation form) 2-7 (preferably 3-5, such as 3, 4,5,6 or 7) (such as when there is 7, number consecutively is b1, b2, b3, b4, b5, b6, b7 to activated carbon chamber； Thickness by that analogy) and along superposed these activated carbon chambers in flow direction (according to this sequentially) of flue gas becomes successively The adjacent activated carbon of top any two of the thick or flow direction along flue gas after first activated carbon chamber (b1) on top The latter thickness of activated carbon chamber (such as b3 or such as b4) is more than or waits in the middle of chamber (such as b2 and b3, or b3 and b4) In the thickness of previous activated carbon chamber (such as b2 or such as b3).
It is preferred that, in the middle of the 2-7 (such as 3) activated carbon chambers of bottom or it is superposed the 2-7 (for example 3) in the middle of activated carbon chamber, according to the order of the flow direction of flue gas, the thickness of second chamber (a2 or b2) is first chamber 1-9 times (such as 1.5-7 times, such as 2,3,4,5 or 6 times) of the thickness of (a1 or b1).Additionally, work as having the 3rd chamber (a3 Or b3) when, the thickness of the 3rd chamber (a3 or b3) be the thickness of second chamber (a2 or b2) 1-2.5 times (preferably 1.2-2 times, Such as 1.3 times, 1.5 times, or 1.8 times).By using said structure design in the application, before chamber solid absorption be situated between Matter (or make solid dielectric, such as activated carbon or activated coke) translational speed more than or equal to back chamber solid absorption medium (or Make solid dielectric) translational speed.
Typically, bottom has 3 activated carbon chambers, according to the order of the flow direction of flue gas, first chamber (a1) (i.e. cup), The thickness of second chamber (a2) (i.e. middle room) and the 3rd chamber (a3) (i.e. rear chamber) be respectively 90-250mm (preferably 100-230mm, such as 120th, 150,200 or 220mm), 360-1000mm (preferably 400-950mm, such as 450,600,700,800 or 900mm) With 432-1200mm (preferably 450-1150mm, such as 500,600,700,800,900,1000 or 1100mm).
Typically, top has 3 activated carbon chambers, according to the order of the flow direction of flue gas, first chamber (b1) (i.e. cup), The thickness of second chamber (b2) (i.e. middle room) and the 3rd chamber (b3) (i.e. rear chamber) be respectively 90-250mm (preferably 100-230mm, such as 120th, 150,200 or 220mm), 360-1000mm (preferably 400-950mm, such as 450,600,700,800 or 900mm) With 432-1200mm (preferably 450-1150mm, such as 500,600,700,800,900,1000 or 1100mm).
It is preferred that, the smoke inlet (1) positioned at the bottom of adsorption tower and the exhanst gas outlet (2) positioned at the top of adsorption tower are in adsorption tower The same side.
It is preferred that, there is a roll feeder (6) in the bottom of each chamber of the active-carbon bed layer segment (A) of bottom.
It is preferred that, there are one or more blowdown rotary valves (7) in the Lower Hold of adsorption tower.
Typically, there are multiple (such as 2-7, such as 3,4,5,6) activated carbon passages (10) in transition region (C).It is preferred that , these activated carbon passages (10) are made up of dividing plate (9) and the tower wall of adsorption tower, or cylinder (9) by circular cross section or Cone cylinder (9) is constituted, or the pipe or cylinder (9) by oval cross section or polygon (such as triangle or rectangle or pentagon or six Side shape) cross section pipe or cylinder (9) constituted.It is further preferred that dividing plate (9) or cylinder (9) or cone cylinder (9) be non-porous plate or It is the cylinder or cone cylinder being made up of imperforate plate.It is further preferred that pipe or cylinder (9) are the pipe or cylinder being made up of imperforate plate.
It is preferred that, 2-7 (preferably 3-5, such as 3,4,5,6 or 7) the activated carbon chamber on top is via respective work Property charcoal passage (10) be communicated to corresponding 2-7 (preferably 3-5, such as 3,4,5,6 or 7) activated carbon of bottom Chamber.
It is preferred that, in the medium position of the vertical direction of transition region (C), the cross-sectional area sum of whole activated carbon passages (10) be less than or Equal to the cross-sectional area sum of whole activated carbon chambers of the cross-sectional area sum or bottom of whole activated carbon chambers on top, preferably , the former is the 20%-60% of the latter, more preferably preferably 20-50%, 22-35%.
The height of the transition region (C) of adsorption tower or the transition region (C) of adsorption tower are 1-5m in the length of vertical direction, preferably 1.2-4m, more preferably 1.5-3m.
It is preferred that, the bottom of each activated carbon chamber on top is equipped with roll feeder (6), it is preferred that these roll feeders (6) In the transition region (C) of adsorption tower and between the active carbon layer of each activated carbon chamber of these roll feeders (6) and bottom (that is, active carbon layer of the roller of roll feeder (6) not with each activated carbon chamber of bottom connects to maintain gap or vertical range Touch).
Typically, the height of the agent structure of adsorption tower is 6-60m (rice), preferably 8-55m (rice), preferably 10-50m, preferably 15-45m, 18-40m, preferably 20-35m, preferably 22-30m.The height of the agent structure of adsorption tower refers to from adsorption tower (main body Structure) import to outlet between height.
Solid absorption medium or solid absorbent (such as activated carbon) in the active-carbon bed layer segment (A) of bottom filling height with Filling (filling) height of solid absorption medium or solid absorbent (such as activated carbon) in the active-carbon bed layer segment (B) on top The ratio between be 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 the activated carbon of broad sense, and it includes：Conventional activated carbon, activated coke, carbon-based absorption is situated between Matter, carbon-supported catalysts, etc..In addition, the activated carbon of solid absorbent or solid absorption medium also alternative above-mentioned broad sense, should This belongs to scope of the claimed in the application.
In addition, in this application, flue gas includes in a broad sense：Conventional industrial smoke or industrial waste gas.
By means of said structure design so that in adsorption tower, each activity of each active carbon bed on top and bottom The respective activated carbon of charcoal bed moves down speed or blanking velocity or activated carbon residence time and can control individually or respectively.In addition, Make it possible to ensure that：It is active-carbon bed with the whole of bottom in whole active carbon beds of unit interval internal upper part in even running The activated carbon blanking total amount of layer is equal.Alternatively, it is also possible to by the roller in active-carbon bed layer segment A (i.e. A beds) only by bottom Formula batcher is controlled.No matter which kind of blanking velocity control mode is used, the solid dielectric translational speed for deferring to above chamber is big In or equal to back chamber solid dielectric translational speed.
According to the second embodiment of the present invention, there is provided a kind of flue gas purifying method of use said apparatus (or it is a kind of using above-mentioned The flue gas of device or the desulphurization and denitration method of sintering flue gas), the method includes：
1) flue gas or sintering flue gas (below, being both referred to as flue gas) are transported to including above-mentioned activated carbon adsorber and (routine) In a kind of activated carbon adsorber of desulphurization and denitration device of Analytic Tower, the flue gas flows successively through the active-carbon bed layer segment (A) of bottom With the active-carbon bed layer segment (B) on top and with the activated carbon being input to from the top of adsorption tower in the two parts (A) and (B) Contacted so that be tightly held by activated carbon including the pollutant including oxysulfide, nitrogen oxides and dioxin；
2) will have been adsorbed from flue gas or sintering flue gas in the activated carbon adsorber of desulphurization and denitration device the activated carbon of pollutant from The bottom of adsorption tower is transferred in a kind of heating zone of activated carbon Analytic Tower of the cooling zone of the heating zone with top and bottom, living Property charcoal with carry out indirect heat exchange as the hot blast of hot gas and be heated or be warming up to activated carbon resolution temperature Td (such as Td= 390-450 DEG C), cause activated carbon to be parsed at a temperature of the Td, regenerated；With
3) activated carbon for parsed in the heating zone on Analytic Tower top, regenerating is via a buffering area for centre i.e. mesozone Section is entered into the cooling zone of Analytic Tower bottom, while by cooling blower using normal temperature air (as cooling wind or cooling air) from solution The cold air inlet in analysis tower cooler area is passed into the cooling zone of Analytic Tower, is carried out indirectly with the activated carbon moved down in cooling zone Heat exchange cools down activated carbon；With
4) activated carbon (for example being removed by screening after deashing) of the cooling for discharging analytically tower bottom is transferred to above step (1) in the top (such as its top feed storehouse) of activated carbon adsorber.
Typically, regenerating active carbon temperature Td is preferably 400-470 DEG C at 390-500 DEG C, more preferably 405-450 DEG C, more excellent It is selected in 410-440 DEG C, more preferably 410-430 DEG C of scope.
Generally, the hot blast in the heating zone of input Analytic Tower has 400~500 DEG C, preferably 410~480 DEG C, more preferably 415-470 DEG C, more preferably 420-460 DEG C, further preferred 420-450 DEG C of temperature.
In the above-mentioned methods, in adsorption tower, each active carbon bed on top and each active carbon bed of bottom are each Activated carbon move down speed or blanking velocity or activated carbon residence time and can control individually or respectively.In even running, It is equal in whole active carbon beds of unit interval internal upper part and the activated carbon blanking total amount of whole active carbon beds of bottom.
Analytic Tower of the invention is the Analytic Tower or regenerator in the dry desulfurization of the exhaust-gas treatment for steel and iron industry, denitrification apparatus, Generally there is 10-45 meters, preferably 15-40 meter, more preferably 20-35 meters of tower height.Desorber generally has 6-100 meters2, it is excellent Select 8-50 meters2, more preferably 10-30 meters2, it is further preferred 15-20 meters2Body cross-section product.And in desulfuring and denitrifying apparatus (desulphurization and denitration) adsorption tower (or reaction tower) generally there is bigger size, the tower height of such as adsorption tower is 6-60m (rice), It is preferred that 8-55m (rice), preferably preferably 10-50m, preferably 15-45m, 18-40m, preferably 20-35m, 22-30m.Adsorption tower Tower height refer to the height that adsorption tower top activated carbon entrance is exported to from absorption tower bottom activated carbon, the i.e. height of the agent structure of tower Degree.
For the design and its absorbing process of flue gas (or waste gas) adsorption tower, there are many documents to have been disclosed in the prior art, See, for example, US5932179, JP2004209332A, and JP3581090B2 (JP2002095930A) and JP3351658B2 (JPH08332347A), JP2005313035A.The application is no longer described in detail.
In the present invention, do not required particularly for Analytic Tower, the Analytic Tower of prior art can be used in the present invention.It is preferred that , Analytic Tower is the vertical Analytic Tower of shell pipe type, and wherein activated carbon is input into from tower top, flows downwardly through tube side, then reaches tower Bottom, and hot gas then flow through shell side, hot gas enter from the side of tower, with the activated carbon for flowing through tube side carry out heat exchange and Cooling, then exports from the opposite side of tower.Preferably, Analytic Tower is the vertical parsing of shell pipe type (or package type) or pipe type Tower, wherein activated carbon from tower top be input into, flow downwardly through the tube side of top heating zone, then reach one in top heating zone with A cushion space between the cooling zone of bottom, then flows through the tube side of bottom cooling zone, then reaches bottom of towe, and hot gas (or High-temperature hot-air) then flow through the shell side of heating zone, the side of hot gas (400-500 DEG C) the analytically heating zone of tower enters, with stream The activated carbon of heated area's tube side carries out indirect heat exchange and lowers the temperature, and is then exported from the opposite side of the heating zone of tower.Cooling wind from The side of the cooling zone of Analytic Tower enters, and indirect heat exchange is carried out with the activated carbon for having parsed, having regenerated for flowing through cooling zone tube side. After the indirect heat exchange, cooling wind is warming up to 120 ± 20 DEG C, such as from about 120 DEG C.
For the design and regeneration method of active carbon of activated carbon Analytic Tower, there are many documents to have been disclosed in the prior art, JP3217627B2 (JPH08155299A) discloses a kind of Analytic Tower (i.e. desorber), and it uses double seal valve, leads to noble gas sealing, Screening, water-cooled (referring to the Fig. 3 in the patent).JP3485453B2 (JPH11104457A) discloses regenerator (referring to the patent Figure 23 and 24), preheating section, double seal valve can be used to lead to noble gas, air cooling or water-cooled.JPS59142824A is disclosed Gas from cooling section is used to preheat activated carbon.Chinese patent application 201210050541.6 (Shanghai Ke Liu companies) is disclosed again The scheme that the energy of raw tower is recycled, which uses drier 2.JPS4918355B is disclosed using blast furnace gas (blast Furnace gas) carry out regenerated carbon.JPH08323144A discloses the regenerator using fuel (heavy oil or light oil), uses Air-heating furnace (referring to Fig. 2 of the patent, 11- hot-blast stoves, 12- fuel supply systems).Chinese utility model 201320075942.7 are related to heater and possess the emission-control equipment (coal-fired, air heating) of the heater, referring to this Fig. 2 in utility model patent.
Analytic Tower of the invention is using air-cooled.
For the situation that Analytic Tower analytic ability is 10t activated carbons per hour, traditional handicraft keeps the temperature in Analytic Tower 420 Coke-stove gas is about 400Nm needed for DEG C3/ h, combustion air is about 2200Nm3/ h, outer thermal wind exhausting is about 2500Nm3/h；It is required Cooling air 30000Nm3/ h, activated carbon temperature is 140 DEG C after cooling.
" optional " expression in this application is with or without, and " optionally " represents and carry out or do not carry out.Analytic Tower can with regenerator Used interchangeably.Regeneration is used interchangeably with parsing.In addition, parsing and desorption are identical concepts." bringing-up section " and " heating zone " It is identical concept." cooling section " and " cooling zone " is identical concept.
The thickness of activated carbon chamber refers to the distance between two porous barriers of the activated carbon chamber or spacing.
Advantages of the present invention or Advantageous Effects
1st, absorption tower of the invention, on the one hand significantly improves treatment quantity, on the other hand, reduce device fabrication and Operation, maintenance cost, save electric energy and heat energy.
2nd, technique is easier control, it is to avoid the dead angle of air-flow occur.
3rd, facility compact, it is easy to maintenance.
4th, the residence time of activated carbon matches very much with the adsorbance of activated carbon in each several part in adsorption tower, and activated carbon utilization rate is high.
5th, reduce the first amount of fill of activated carbon, reduce cost of investment, while reduce not with activated carbon the stopping in tower of smoke contacts Stay the time.
Brief description of the drawings
Fig. 1 is the desulfuring and denitrifying apparatus and process flow diagram including activated carbon adsorber and regenerating active carbon tower of prior art.
Fig. 2 is the schematic diagram of the adsorption tower of prior art.
Fig. 3 is the schematic diagram of another adsorption tower of prior art.
Fig. 4, Fig. 5 and Fig. 6 are the schematic diagrames of three kinds of adsorption towers of the invention.
Reference：
A, the active-carbon bed layer segment of bottom, B, the active-carbon bed layer segment on top, C, the transition region in the middle part of adsorption tower, 1st, smoke inlet, 2, exhanst gas outlet, 3, feeding warehouse, 4, porous barrier, 4 ', porous barrier or shutter, 5, flue gas Passage, 6, roll feeder, 7, rotary valve, 8, conveying device, 9, non-porous dividing plate or the cylinder being made up of imperforate plate or Cone cylinder, 10, the activated carbon passage in transition region (C).
A1, the first activated carbon chamber of bottom, a2, the second activated carbon chamber of bottom, a3, the 3rd activated carbon chamber of bottom Room, b1, the first activated carbon chamber on top, b2, the second activated carbon chamber on top, b3, the 3rd activated carbon chamber on top.
The flue gas upstream end of G1, the active-carbon bed layer segment (A) of bottom, G2, the flue gas stream of the active-carbon bed layer segment (A) of bottom Go out end, G3, the flue gas upstream end of the active-carbon bed layer segment (B) on top, G4, the flue gas of the active-carbon bed layer segment (B) on top Outflow end.
Specific embodiment
Desulphurization and denitration device used in embodiment includes activated carbon adsorber and Analytic Tower.Activated carbon Analytic Tower has upper The heating zone in portion and the cooling zone of bottom and positioned at intermediate buffer between the two.
It is the sintering device flue gas from steel and iron industry that sintering flue gas to be processed is needed in embodiment.
In embodiment, the size of Analytic Tower is：20 meters of tower height, body cross-section product is 15m2。
Three kinds of structures of adsorption tower are referring to Fig. 4-6.
A kind of activated carbon method smoke eliminator (that is, one kind including activated carbon adsorber and Analytic Tower including activated carbon adsorber Desulphurization and denitration device or a kind of activated carbon method smoke eliminator including activated carbon adsorber and Analytic Tower), the charcoal absorption Tower includes active-carbon bed layer segment (A), the active-carbon bed layer segment (B) on top and the transition between the two parts of bottom Area (C) (or making mesozone (C)), and the activated carbon adsorber include positioned at adsorption tower top or top feeding warehouse (3), Smoke inlet (1) positioned at the bottom of adsorption tower and the exhanst gas outlet (2) positioned at the top of adsorption tower, its middle and lower part it is active-carbon bed The flue gas outflow end (G2) of layer segment (A) passes through exhaust gases passes (5) with the flue gas upstream end (G3) of the active-carbon bed layer segment (B) on top It is connected, the active-carbon bed layer segment (A) of bottom has by 2-7 (preferably 3-5 of porous barrier (4) isolation (or isolation is formed) Individual, such as 3,4,5,6 or 7) activated carbon chamber (such as when there is 7, number consecutively is a1, a2, a3, a4, A5, a6, a7；Flow direction (according to this sequentially) by that analogy) and along flue gas is located at these activated carbon chambers of bottom The bottom any two phase that thickness is thickening successively or flow direction along flue gas is after first activated carbon chamber (a1) of bottom The latter thickness of activated carbon chamber (such as a3 or such as a4) in the middle of adjacent activated carbon chamber (such as a2 and a3, or a3 and a4) Degree is more than or equal to the thickness of previous activated carbon chamber (such as a2 or such as a3), active-carbon bed layer segment (B) tool on top Have by 2-7 (preferably 3-5, such as 3,4,5,6 or 7) activated carbon of porous barrier (4) isolation (or isolation is formed) (such as when there is 7, number consecutively is b1, b2, b3, b4, b5, b6, b7 to chamber；By that analogy) and along flue gas Superposed these activated carbon chambers in flow direction (according to this sequentially) thickness is thickening successively or flow direction along flue gas Top any two after first activated carbon chamber (b1) on top adjacent activated carbon chamber (such as b2 and b3, or b3 And b4) in the middle of latter thickness of activated carbon chamber (such as b3 or such as b4) more than or equal to previous activated carbon chamber (for example B2 or such as b3) thickness.
It is preferred that, in the middle of the 2-7 (such as 3) activated carbon chambers of bottom or it is superposed the 2-7 (for example 3) in the middle of activated carbon chamber, according to the order of the flow direction of flue gas, the thickness of second chamber (a2 or b2) is first chamber 1-9 times (such as 1.5-7 times, such as 2,3,4,5 or 6 times) of the thickness of (a1 or b1).Additionally, work as having the 3rd chamber (a3 Or b3) when, the thickness of the 3rd chamber (a3 or b3) be the thickness of second chamber (a2 or b2) 1-2.5 times (preferably 1.2-2 times, Such as 1.3 times, 1.5 times, or 1.8 times).
Typically, bottom has 3 activated carbon chambers, according to the order of the flow direction of flue gas, first chamber (a1) (i.e. cup), The thickness of second chamber (a2) (i.e. middle room) and the 3rd chamber (a3) (i.e. rear chamber) be respectively 90-250mm (preferably 100-230mm, such as 120th, 150,200 or 220mm), 360-1000mm (preferably 400-950mm, such as 450,600,700,800 or 900mm) With 432-1200mm (preferably 450-1150mm, such as 500,600,700,800,900,1000 or 1100mm).
Typically, top has 3 activated carbon chambers, according to the order of the flow direction of flue gas, first chamber (b1) (i.e. cup), The thickness of second chamber (b2) (i.e. middle room) and the 3rd chamber (b3) (i.e. rear chamber) be respectively 90-250mm (preferably 100-230mm, such as 120th, 150,200 or 220mm), 360-1000mm (preferably 400-950mm, such as 450,600,700,800 or 900mm) With 432-1200mm (preferably 450-1150mm, such as 500,600,700,800,900,1000 or 1100mm).
It is preferred that, the smoke inlet (1) positioned at the bottom of adsorption tower and the exhanst gas outlet (2) positioned at the top of adsorption tower are in adsorption tower The same side.
It is preferred that, there is a roll feeder (6) in the bottom of each chamber of the active-carbon bed layer segment (A) of bottom.
It is preferred that, there are one or more blowdown rotary valves (7) in the Lower Hold of adsorption tower.
Typically, there are multiple (such as 2-7, such as 3,4,5,6) activated carbon passages (10) in transition region (C).It is preferred that , these activated carbon passages (10) are made up of dividing plate (9) and the tower wall of adsorption tower, or cylinder (9) by circular cross section or Cone cylinder (9) is constituted, or the pipe or cylinder (9) by oval cross section or polygon (such as triangle or rectangle or pentagon or six Side shape) cross section pipe or cylinder (9) constituted.It is further preferred that dividing plate (9) or cylinder (9) or cone cylinder (9) be non-porous plate or It is the cylinder or cone cylinder being made up of imperforate plate.It is further preferred that pipe or cylinder (9) are the pipe or cylinder being made up of imperforate plate.
It is preferred that, 2-7 (preferably 3-5, such as 3,4,5,6 or 7) the activated carbon chamber on top is via respective work Property charcoal passage (10) be communicated to corresponding 2-7 (preferably 3-5, such as 3,4,5,6 or 7) activated carbon of bottom Chamber.
It is preferred that, in the medium position of the vertical direction of transition region (C), the cross-sectional area sum of whole activated carbon passages (10) be less than or Equal to the cross-sectional area sum of whole activated carbon chambers of the cross-sectional area sum or bottom of whole activated carbon chambers on top, preferably , the former is the 20%-60% of the latter, preferably 20-50%.
The height of the transition region (C) of adsorption tower or the transition region (C) of adsorption tower are 1-5m in the length of vertical direction, preferably 1.2-4m, more preferably 1.5-3m.
It is preferred that, the bottom of each activated carbon chamber on top is equipped with roll feeder (6), it is preferred that these roll feeders (6) In the transition region (C) of adsorption tower and between the active carbon layer of each activated carbon chamber of these roll feeders (6) and bottom (that is, active carbon layer of the roller of roll feeder (6) not with each activated carbon chamber of bottom connects to maintain gap or vertical range Touch).
Typically, the height of the agent structure of adsorption tower is 6-60m (rice), preferably 8-55m (rice), preferably 10-50m, preferably 15-45m, 18-40m, preferably 20-35m, preferably 22-30m.
According to the second embodiment of the present invention, there is provided a kind of gas cleaning of use said apparatus (or it is sintering flue gas desulfurization, de- Nitre method), the method includes：
1) flue gas that (contains pollutant) or sintering flue gas (below, being both referred to as flue gas) are transported to and are inhaled including above-mentioned activated carbon In a kind of activated carbon adsorber of desulphurization and denitration device of attached tower and (routine) Analytic Tower, the flue gas flows successively through the activity of bottom The active-carbon bed layer segment (B) on charcoal bed part (A) and top and be input to from the top of adsorption tower the two parts (A) and (B) activated carbon in is contacted so that be tightly held by activated carbon including the pollutant including oxysulfide, nitrogen oxides and dioxin；
2) will have been adsorbed from flue gas or sintering flue gas in the activated carbon adsorber of desulphurization and denitration device the activated carbon of pollutant from The bottom of adsorption tower is transferred in a kind of heating zone of activated carbon Analytic Tower of the cooling zone of the heating zone with top and bottom, living Property charcoal with carry out indirect heat exchange as the hot blast of hot gas and be heated or be warming up to activated carbon resolution temperature Td (such as Td= 390-450 DEG C), cause activated carbon to be parsed at a temperature of the Td, regenerated；With
3) activated carbon for parsed in the heating zone on Analytic Tower top, regenerating is via a buffering area for centre i.e. mesozone Section is entered into the cooling zone of Analytic Tower bottom, while by cooling blower using normal temperature air (as cooling wind or cooling air) from solution The cold air inlet in analysis tower cooler area is passed into the cooling zone of Analytic Tower, is carried out indirectly with the activated carbon moved down in cooling zone Heat exchange cools down activated carbon；With
4) activated carbon (for example being removed by screening after deashing) of the cooling for discharging analytically tower bottom is transferred to above step (1) in the top (such as its top feed storehouse) of activated carbon adsorber.
Typically, regenerating active carbon temperature Td is preferably 400-470 DEG C at 390-500 DEG C, more preferably 405-450 DEG C, more excellent It is selected in 410-440 DEG C, more preferably 410-430 DEG C of scope.
Generally, the hot blast in the heating zone of input Analytic Tower has 400~500 DEG C, preferably 410~480 DEG C, more preferably 415-470 DEG C, more preferably 420-460 DEG C, further preferred 420-450 DEG C of temperature.
Embodiment 1
Adsorption tower is as shown in Figure 4.Desulphurization and denitration device includes activated carbon adsorber (30 meters of tower height, cross-sectional area 120m2) and Analytic Tower (20 meters of tower height, cross-sectional area 15m2)。
The active-carbon bed layer segment A of bottom has the active-carbon bed layer segment B on three activated carbon chamber a1, a2 and a3 and top With three activated carbon chambers b1, b2 and b3.
Along airflow direction, the tandem of flue gas is contacted by each layer of activated carbon, define each floor be respectively lower floor's cup, middle room, Rear chamber；Upper strata cup, middle room, rear chamber.Room thickness is respectively 150mm, 450mm, 900mm, total thickness before, during and after lower floor Degree 1500mm；Room thickness is respectively 150mm, 450mm, 900mm, gross thickness 1500mm before, during and after upper strata；So as to controllable The toxicity charcoal residence time is such as 40h, 120h, 240h before, during and after making upper and lower layer.
Upper bottom discharge can adjust.
Adsorption tower is divided into upper and lower two-layer by the device of the present embodiment, and each layer activated carbon is divided into multicell, each room lower section using porous barrier Control each toxicity charcoal flowing velocity (or residence time) respectively using roll feeder.
Activated carbon chamber a1 or b1 preferentially with smoke contacts is relatively thin, takes blanking velocity faster, makes the activated carbon of adsorption saturation Discharge as early as possible；Activated carbon chamber in each layer finally with smoke contacts is thicker, and the residence time is more long indoors for activated carbon, can effectively drop Low kind of dust.
In the medium position of the vertical direction of transition region C, the cross-sectional area sum of whole activated carbon passages 10 is the whole living of top 55% or so of the cross-sectional area sum of whole activated carbon chambers of the cross-sectional area sum or bottom of property charcoal chamber.The mistake of adsorption tower It is 2m in the length of vertical direction to cross the height in area (C) or the transition region (C) of adsorption tower.
After upper strata activated carbon is discharged through roll feeder, the top for being placed in lower floor's activated carbon chamber stores temporarily.
The rod bottom of roll feeder does not contact with activated carbon, prevents round roller from producing high temperature or spark with activated carbon friction.
Embodiment 2
Adsorption tower is as shown in Figure 5.The flue gas little for pollutant component fluctuation, can remove the roll feeder of upper strata blanking from, The residence time of material in each floor is realized by controlling the width of each room of levels.The height or adsorption tower of the transition region (C) of adsorption tower Transition region (C) be 3m in the length of vertical direction.
Along airflow direction, the tandem of flue gas is contacted by each layer of activated carbon, define each floor be respectively lower floor's cup, middle room, Rear chamber；Upper strata cup, middle room, rear chamber.Room thickness is respectively 150mm, 450mm, 900mm, total thickness before, during and after lower floor Degree 1500mm；Room thickness is respectively 150mm, 450mm, 900mm, gross thickness 1500mm before, during and after upper strata；So as to controllable The toxicity charcoal residence time is such as 40h, 120h, 240h before, during and after making upper and lower layer.
Embodiment 3
Adsorption tower is as shown in Figure 6.In order to reduce the first amount of fill of activated carbon, cost of investment is reduced, while reduction does not connect with flue gas Residence time of the tactile activated carbon in tower, can be by the length reduction of the activated carbon passage in the middle of levels.
Along airflow direction, the tandem of flue gas is contacted by each layer of activated carbon, define each floor be respectively lower floor's cup, middle room, Rear chamber；Upper strata cup, middle room, rear chamber.Room thickness is respectively 150mm, 450mm, 900mm, total thickness before, during and after lower floor Degree 1500mm；Room thickness is respectively 150mm, 450mm, 900mm, gross thickness 1500mm before, during and after upper strata；So as to controllable The toxicity charcoal residence time is such as 40h, 120h, 240h before, during and after making upper and lower layer.
Intermediate active charcoal passage 10 is invalid, so on the premise of activated carbon blanking velocity (resistance is small) is ensured, also The height (or length) and total cross-section area of its (activated carbon passage) are reduced as far as possible.At the middle position of the vertical direction of transition region C Put, the cross-sectional area sum of whole activated carbon passages 10 be whole activated carbon chambers on top cross-sectional area sum or bottom it is complete The 22% of the cross-sectional area sum of portion's activated carbon chamber.The height of the transition region (C) of adsorption tower or the transition region (C) of adsorption tower are being hung down Nogata to length be 1.8m.

Claims (10)

1. a kind of activated carbon method smoke eliminator of activated carbon adsorber is included, the activated carbon adsorber includes the activated carbon of bottom Bed part (A), the active-carbon bed layer segment (B) on top and the transition region (C) between the two parts, and the activated carbon Adsorption tower includes the feeding warehouse (3) positioned at the top of adsorption tower or top, the smoke inlet (1) positioned at the bottom of adsorption tower and is located at The exhanst gas outlet (2) on the top of adsorption tower, the flue gas outflow end (G2) of the active-carbon bed layer segment (A) of its middle and lower part and the work on top The flue gas upstream end (G3) of property charcoal bed part (B) is connected by exhaust gases passes (5), and the active-carbon bed layer segment (A) of bottom has 2-7 (preferably 3-5) the activated carbon chamber isolated by porous barrier (4), and, active-carbon bed layer segment (B) tool on top There is 2-7 (preferably 3-5) the activated carbon chamber isolated by porous barrier (4).
2. purifier according to claim 1, the active-carbon bed layer segment (A) of its middle and lower part has by porous barrier (4) The 2-7 of isolation (preferably 3-5) the activated carbon chamber and flow direction along flue gas is located at these activated carbon chambers of bottom The bottom any two that thickness is thickening successively or flow direction along flue gas is after first activated carbon chamber (a1) of bottom In the middle of adjacent activated carbon chamber latter thickness of activated carbon chamber more than or equal to previous activated carbon chamber thickness, top Active-carbon bed layer segment (B) have 2-7 (preferably 3-5) the activated carbon chamber isolated by porous barrier (4) and along The thickness of superposed these activated carbon chambers in flow direction of flue gas is thickening successively or flow direction along flue gas is on top The latter thickness of activated carbon chamber in the middle of the adjacent activated carbon chamber of top any two after first activated carbon chamber (b1) More than or equal to the thickness of previous activated carbon chamber；Preferably, wherein the 2-7 (such as 3) positioned at bottom are living Property charcoal chamber in the middle of or the superposed 2-7 (such as 3) activated carbon chamber in the middle of, according to the flow direction of flue gas Sequentially, the thickness of second chamber (a2 or b2) is 1-9 times of (such as 1.5-7 times, such as 2 of the thickness of first chamber (a1 or b1) Or 3 times), and when there is the 3rd chamber (a3 or b3), the thickness of the 3rd chamber (a3 or b3) is second chamber (a2 or b2) Thickness 1-2.5 times (preferably 1.2-2 times, such as 1.3 times, 1.5 times, or 1.8 times).
3. purifier according to claim 2, its middle and lower part has 3 activated carbon chambers, according to the flowing side of flue gas To order, the thickness of first chamber (a1) (i.e. cup), second chamber (a2) (i.e. middle room) and the 3rd chamber (a3) (i.e. rear chamber) Be respectively 90-250mm (preferably 100-230mm, such as 120,150,200 or 220mm), 360-1000mm (preferably 400-950mm, Such as 450,600,700,800 or 900mm) and 432-1200mm (preferably 450-1150mm, such as 500,600,700,800, 900th, 1000 or 1100mm)；And/or
Top has 3 activated carbon chambers, according to the order of the flow direction of flue gas, first chamber (b1) (i.e. cup), second The thickness of chamber (b2) (i.e. middle room) and the 3rd chamber (b3) (i.e. rear chamber) be respectively 90-250mm (preferably 100-230mm, such as 120, 150th, 200 or 220mm), 360-1000mm (preferably 400-950mm, such as 450,600,700,800 or 900mm) and 432-1200mm (preferably 450-1150mm, such as 500,600,700,800,900,1000 or 1100mm).
4. the purifier according to any one of claim 1-3, wherein positioned at the smoke inlet (1) of the bottom of adsorption tower With the same side of exhanst gas outlet (2) in adsorption tower positioned at the top of adsorption tower.
5. the purifier according to any one of claim 1-4, wherein in the active-carbon bed layer segment (A) of bottom The bottom of each chamber has a roll feeder (6)；And/or
There are one or more blowdown rotary valves (7) in the Lower Hold of adsorption tower.
6. the purifier according to any one of claim 1-5, wherein having multiple activated carbons in transition region (C) Passage (10)；Preferably, these activated carbon passages (10) are made up of dividing plate (9) and the tower wall of adsorption tower, or by rounded cross section The cylinder (9) or cone cylinder (9) in face are constituted, or by the pipe or cylinder (9) or the pipe or cylinder of polygonal crosssection of oval cross section (9) constituted；It is further preferred that dividing plate (9) or cylinder (9) or cone cylinder (9) are non-porous plate or the cylinder being made up of imperforate plate Or cone cylinder, pipe or cylinder (9) they are the pipe or cylinder being made up of imperforate plate.
7. the purifier according to any one of claim 1-6,2-7 (preferably 3-5, example of its middle and upper part Such as 3,4,5,6 or 7) activated carbon chamber is communicated to corresponding 2-7 of bottom via respective activated carbon passage (10) (preferably 3-5, such as 3,4,5,6 or 7) activated carbon chamber.
8. the purifier according to any one of claim 1-7, wherein the middle part of the vertical direction in transition region (C) Position, the cross-sectional area sum of whole activated carbon passages (10) less than or equal to whole activated carbon chambers on top cross-sectional area it And/or the cross-sectional area sum of whole activated carbon chambers of bottom, it is preferred that the former is the 20%-60% of the latter.
9. the purifier according to any one of claim 1-8, the bottom dress of each activated carbon chamber of its middle and upper part There is roll feeder (6), it is preferred that these roll feeders (6) are in the transition region (C) of adsorption tower and these roll-types are given Gap or vertical range (that is, roll feeder (6) are maintained between the active carbon layer of each activated carbon chamber of material machine (6) and bottom Active carbon layer of the roller not with each activated carbon chamber of bottom contact).
10. using flue gas purifying method (or sintering flue gas desulfurization, the denitration side of the device any one of claim 1-9 Method), the method includes：
1) flue gas or sintering flue gas (below, being both referred to as flue gas) are transported to including any one of claim 1-9 In a kind of activated carbon adsorber of desulphurization and denitration device of activated carbon adsorber and Analytic Tower, the flue gas flows successively through the work of bottom The active-carbon bed layer segment (B) on property charcoal bed part (A) and top and with the two parts (A) are input to from the top of adsorption tower Activated carbon in (B) is contacted so that inhaled by activated carbon including the pollutant including oxysulfide, nitrogen oxides and dioxin It is attached；
2) will have been adsorbed from flue gas or sintering flue gas in the activated carbon adsorber of desulphurization and denitration device the activated carbon of pollutant from The bottom of adsorption tower is transferred in a kind of heating zone of activated carbon Analytic Tower of the cooling zone of the heating zone with top and bottom, living Property charcoal with carry out indirect heat exchange as the hot blast of hot gas and be heated or be warming up to activated carbon resolution temperature Td (such as Td= 390-450 DEG C), cause activated carbon to be parsed at a temperature of the Td, regenerated；With
3) activated carbon for parsed in the heating zone on Analytic Tower top, regenerating is via a buffering area for centre i.e. mesozone Section is entered into the cooling zone of Analytic Tower bottom, while by cooling blower using normal temperature air (as cooling wind or cooling air) from solution The cold air inlet in analysis tower cooler area is passed into the cooling zone of Analytic Tower, is carried out indirectly with the activated carbon moved down in cooling zone Heat exchange cools down activated carbon；With
4) activated carbon (for example being removed by screening after deashing) of the cooling for discharging analytically tower bottom is transferred to above step (1) in the top (such as its top feed storehouse) of activated carbon adsorber.
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