CN204502749U

CN204502749U - Use the flue gas desulfurization and denitrification device of the two adsorption tower of series connection

Info

Publication number: CN204502749U
Application number: CN201420735275.5U
Authority: CN
Inventors: 魏进超; 张震; 叶恒棣; 孙英; 李俊杰
Original assignee: Zhongye Changtian International Engineering Co Ltd
Current assignee: Zhongye Changtian International Engineering Co Ltd
Priority date: 2014-11-28
Filing date: 2014-11-28
Publication date: 2015-07-29
Anticipated expiration: 2024-11-28

Abstract

There is provided a kind of comprise series connection double activated carbon adsorption tower (1) and (1a) and comprise the flue gas desulfurization and denitrification device of flue gas temperature controlling instruments, this device comprises: first adsorption tower (1) of series connection and the second adsorption tower (1a); Regenerating active carbon tower (2); Former flue gas conveying flue (102) and flue (102a), neat stress pipeline (102b), neat stress pipeline (102c), ammonia transfer pipeline (106), the cold air inlet (P1) that conveying flue (102) is provided with and fresh water (FW) nozzle (P2); Fresh water (FW) conveyance conduit (508), the other end of this pipeline (508) is connected to the ammonia-containing water basin in relieving haperacidity district.Adopt double activated carbon adsorption tower (1) and (1a) of series connection, significantly improve the denitration rate of device.

Description

Use the flue gas desulfurization and denitrification device of the two adsorption tower of series connection

Technical field

The utility model relates to the flue gas desulfurization and denitration method and device that adopt series connection double activated carbon adsorption tower (also referred to as reaction tower).More particularly, the utility model relate to adopt series connection double activated carbon adsorption tower and the measure that in the upstream of activated carbon adsorber or front end, spray cooling be have employed to flue gas (sinter fume) simultaneously and convert cold wind cooling to control the temperature of active carbon bed in adsorption tower 110 ~ 160 DEG C of scopes, preferably control the method 120 ~ 150 DEG C of scopes, and the method for many in adsorption tower (position) some spray ammonia, these belong to sinter fume process field.

Background technology

For the sintering device flue gas of industrial smoke, especially steel and iron industry, the large-scale dry desulfurization, denitrification apparatus and the technique that comprise activated carbon adsorber and Analytic Tower is adopted to be more satisfactory.

Active carbon flue gases purification have can simultaneous SO_2 and NO removal, realize by-product resource, adsorbent can be recycled, denitrification efficiency high, is the desulfurization and denitrification integral technology very with development prospect.In the desulphurization and denitration device comprising activated carbon adsorber and Analytic Tower (or regenerator), activated carbon adsorber is used for the pollutant comprising oxysulfide, nitrogen oxide and dioxin from sinter fume or waste gas (especially the sinter fume of the sintering machine of steel and iron industry) absorption, and Analytic Tower is used for the hot recycling of active carbon.

Activated carbon method flue gases purification has the function of simultaneous SO_2 and NO removal, and the main equipment that this technique comprises has adsorption tower, regenerator and active carbon conveying device.For NOx, SO ₂more easily remove, next group adsorption tower of normal condition can obtain the desulfurization degree up to 90%, but denitration rate is lower.

In addition, for the desulphurization denitration tower highly arriving tens meters, in adsorption tower, the temperature of active carbon bed controls to face huge challenge.

For activated carbon method flue gases purification, in activated carbon adsorber, the normal working temperature of active carbon bed is 110 ~ 160 DEG C, preferably controls at 120 ~ 150 DEG C.

On the one hand, in order to prevent the active carbon in bed from burning, strict control active carbon bed temperature lower than 165 DEG C, preferably lower than 160 DEG C, more preferably less than 150 DEG C.This is because, although the burning-point of active carbon is at about 430 DEG C, but be generally exothermic reaction at the chemical reaction that activated carbon surface occurs, and containing inflammable, combustion-supporting material on a small quantity in dust in flue gas, and active carbon itself also carries inflammability dust secretly.If strictly do not control the temperature in adsorption tower, then the existence of these flammable material or inflammability dust causes potential safety hazard at any time, light then active carbon spontaneous combustion in the adsorption tower that may cause tens meters high, serious then cause dust explosion, the appearance of these two kinds of accidents is all catastrophic for large-scale desulphurization denitration tower apparatus.So for the sake of security, generally arranging active carbon bed temperature alarming temperature is 165 DEG C.Sinter former flue gas temperature after booster fan pressurization to be generally 100 DEG C-220 DEG C, to be more generally between 110-180 DEG C, and oxygen content is high in sinter fume, in tower, after activated carbon surface oxidation, bed temperature can exceed 5-15 DEG C than input gas temperature, therefore in order to ensure the safe operation of desulfuring and denitrifying apparatus, need to control active carbon bed temperature.In addition, before adsorption tower is stopped transport, active carbon bed temperature in tower must be kept lower than 80 DEG C, now to need to cool to active carbon bed, therefore stop transport in order to ensure safety, also must control active carbon bed temperature.

On the other hand, need strict control active carbon bed temperature higher than or be not less than 110 DEG C, preferably higher than or be not less than 120 DEG C, more preferably higher than or be not less than 125 DEG C.This is because, if bed temperature lower than 110 DEG C, especially lower than 100 DEG C, then enter the temperature of water vapour contained in the sinter fume in bed close to dew point (or set point), very easily become water and react with oxysulfide the acid becoming severe corrosive, cause the heavy corrosion of device and seriously reduce the effect of denitration, denitration.

Traditional flue gas cool-down method is to spray cooling in flue gas.This cooling means can effectively control active carbon bed temperature when system is normally run, but smoke moisture can be caused too high for cooling before system shutdown, causes active carbon can adsorb a large amount of steam in flue gas, reduces active carbon low-temperature denitration active.

Usually, activated carbon method flue gases purification has the features such as desulphurization denitration rate is high, accessory substance resourcebility utilizes, active carbon can be recycled, and the principle of its desulphurization denitration is as follows:

At the surperficial SO of active carbon ₂oxidized absorption forms sulfuric acid, its reaction equation:

2SO ₂+O ₂+2H ₂O→2H ₂SO ₄

If spray into a small amount of ammonia in flue gas, SO can be accelerated ₂absorption, its reaction equation:

NH ₃+H ₂SO ₄→NH ₄HSO ₄

But, in order to reach the effect of denitration while desulfurization, generally can spray more ammonia at adsorption tower smoke inlet place, the ammonia needed for desulfurization should be met, meet the ammonia needed for denitration simultaneously.Denitration reaction formula is:

4NO+O ₂+4NH ₃→4N ₂+6H ₂O

Meanwhile in adsorption tower, also there is following side reaction:

2NH ₃+H ₂SO ₄→(NH ₄) ₂SO ₄

And SO ₂with NH ₃reaction rate than NO and NH ₃reaction rate faster, SO ₂existence inhibit the carrying out of denitration reaction.In addition, the SO in flue gas ₃, HF and HCl also can react with NH3, for denitration, these side reactions can considerably increase the consumption of ammonia, add operating cost.

In order to obtain higher denitration rate, can carry out plural serial stage to adsorption tower is the direction of making great efforts, and finally realizes pollutant discharge in compliance with the standard.

Utility model content

The purpose of this utility model carries out plural serial stage to adsorption tower, to obtain higher denitration rate, finally realizes pollutant discharge in compliance with the standard.

Meanwhile, the utility model also provides a kind of control method of active carbon bed temperature, and can guarantee that system realizes temperature safely and effectively and controls when running and stop transport, Accident prevention occurs.The measure that have employed spray cooling in the upstream of activated carbon adsorber or front end to flue gas (sinter fume) simultaneously and convert cold wind cooling, to control the temperature of active carbon bed in adsorption tower 110 ~ 160 DEG C of scopes, preferably controls the method 120 ~ 150 DEG C of scopes.

Active carbon bed temperature-controlled process used in this application have employed simultaneously and carries out spray cooling and convert cold wind lowering the temperature to flue gas.When adsorption tower normally works, if active carbon bed temperature is higher than 150 DEG C, then before utilizing adsorption tower, the injection point that arranges after booster fan, in former flue gas, spray into atomized water flue gas is lowered the temperature, thus reduce active carbon bed temperature.The amount of the fresh water (FW) sprayed is determined by exhaust gas volumn and flue-gas temperature.

Adsorption tower normally stop transport or under accident conditions (device because of fault or maintenance need shut down; or during water-cooling system fault); in order to reduce temperature in adsorption tower under the condition not increasing tower humidity; close fresh water (FW) cooling system; former gas baffle is closed; open cold blast sliding valve, in flue, pass into cold air, thus reduce active carbon bed temperature in adsorption tower.

In addition, the utility model is also used in multidigit point in activated carbon adsorber and sprays the means of Dilution air ammonia, and it is used for the effect simultaneously taking into account desulfurization and denitration on the one hand, on the other hand, also assists adjustment and/or the control of temperature in adsorption tower.Alternatively, as preferred scheme of the present utility model, adopt the flue-gas temperature that three kinds of means or measure control in adsorption tower, to adsorb under desirable flue-gas temperature.

According to first embodiment of the present utility model, provide the desulfuring and denitrifying apparatus comprising the two adsorption tower of series connection, it comprises

1) first adsorption tower of connecting and the second adsorption tower,

2) regenerating active carbon tower (or Analytic Tower),

3) at the former flue gas conveying flue of the upstream, flue gas input port of the first adsorption tower, this flue is provided with cold air inlet (P1) and/or fresh water (FW) nozzle (P2),

4) one-level flue, its front end is connected to the exhanst gas outlet of the first adsorption tower and its rear end are connected to the second adsorption tower inlet plenum via second baffle door,

5) secondary neat stress pipeline, its front end is connected to the exhanst gas outlet of the first adsorption tower and its rear end is communicated to blowdown stack via third gear plate door,

6) three grades of neat stress pipelines, its front end is connected to the exhanst gas outlet of the second adsorption tower and its rear end is communicated to blowdown stack via fourth gear plate door, and

7) ammonia transfer pipeline, wherein: on ammonia transfer pipeline, (such as middle section position) is provided with a kind of ammonia and air mixing device (M), the rear end of this ammonia transfer pipeline is communicated to former flue gas conveying flue and one-level flue respectively and/or extends in the first adsorption tower and/or the second adsorption tower and to have installed ammonia nozzle at the end of ammonia transfer pipeline, or separate multiple ammonia branch road from the latter end of this ammonia transfer pipeline, these branch roads are communicated to multiple ammonia nozzle in former flue gas conveying flue and one-level flue and the one or more ammonia nozzle be optionally connected in the inlet plenum of the first adsorption tower and the second adsorption tower and optional clearance space between each active carbon bed of the first adsorption tower or the second adsorption tower or spray ammonia pipe array (as 106a and 106b) respectively, such as, by dilute former flue gas input channel neutralization that ammonia (such as via the first ammonia valve V4) passes into the first adsorption tower optionally (such as via the second ammonia valve V5) pass in the one-level flue of the second adsorption tower and be optionally passed in the first adsorption tower and/or the second adsorption tower,

The flue of its Central Plains flue gas is communicated to the air inlet of the first adsorption tower via the first baffle door, the exhaust uptake of drawing from the gas outlet of the first adsorption tower is divided into the first branch road (i.e. one-level flue) and the second branch road (i.e. secondary smoke pipeline) two branch roads, wherein the first branch road (i.e. one-level flue) is communicated to the air inlet of the second adsorption tower via second baffle door, second branch road (i.e. secondary smoke pipeline) is communicated to blowdown stack via third gear plate door

The exhaust uptake of drawing from the gas outlet of the second adsorption tower is communicated to above-mentioned blowdown stack via fourth gear plate door,

The active carbon of discharging from the bottom of the first adsorption tower is transported to the top of regenerator by the 3rd (3#) active carbon conveyer, the thick activated carbon granule that the regenerated carbon of discharging from the bottom of regenerator obtains after bolting is transported to the top of the first adsorption tower and/or the second adsorption tower by first (1#) active carbon conveyer, and the active carbon of discharging from the bottom of the second adsorption tower is transported to the top of the first adsorption tower by second (2#) active carbon conveyer.

Preferably, the first adsorption tower and the second adsorption tower have one or more active carbon bed respectively, a preferred 2-5 bed.

First adsorption tower and the second adsorption tower have identical or different structure and size each other.

Preferably, ammonia nozzle is provided with in the inlet plenum of the first adsorption tower and/or the second adsorption tower, spray ammonia pipe array (as 106a and 106b) is arranged it is further preferred that be provided with in ammonia nozzle and the clearance space in the first adsorption tower (1) and/or the second adsorption tower between each bed in the inlet plenum of the first adsorption tower and/or the second adsorption tower.Each branch road of (dilution) ammonia transfer pipeline is connected with these nozzles respectively.

According to second embodiment of the present utility model, provide the desulfuring and denitrifying apparatus comprising the two adsorption tower of series connection, it comprises

1) first adsorption tower of connecting and the second adsorption tower,

2) regenerating active carbon tower (or Analytic Tower),

3) at the former flue gas conveying flue of the upstream, flue gas input port of the first adsorption tower,

7) ammonia transfer pipeline, wherein: on this ammonia transfer pipeline, (such as middle section position) is provided with a kind of ammonia and air mixing device (M), the rear end of this ammonia transfer pipeline is communicated to former flue gas conveying flue and one-level flue respectively and/or extends in the first adsorption tower and the second adsorption tower and to have installed ammonia nozzle at the end of ammonia transfer pipeline, or separate multiple ammonia branch road from the latter end of this ammonia transfer pipeline, these branch roads are communicated to multiple ammonia nozzle in former flue gas conveying flue and one-level flue and the one or more ammonia nozzle be optionally connected in the inlet plenum of the first adsorption tower and the second adsorption tower and optional clearance space between each active carbon bed of the first adsorption tower or the second adsorption tower or spray ammonia pipe array (as 106a and 106b) respectively, such as, by dilute former flue gas input channel neutralization that ammonia (such as via ammonia first valve V4) passes into the first adsorption tower optionally (such as via the second ammonia valve V5) pass in the one-level flue of the second adsorption tower and be optionally passed in the first adsorption tower and/or the second adsorption tower,

The active carbon of discharging from the bottom of the first adsorption tower is transported to the top of regenerator by the 3rd (3#) active carbon conveyer, the thick activated carbon granule that the regenerated carbon of discharging from the bottom of regenerator obtains after bolting is transported to the top of the first adsorption tower and/or the second adsorption tower by first (1#) active carbon conveyer, and the active carbon of discharging from the bottom of the second adsorption tower is transported to the top of the first adsorption tower by second (2#) active carbon conveyer;

8) cold air inlet be provided with on the upstream position P 1 of former flue gas conveying flue, and the fresh water (FW) nozzle be provided with on the downstream position P2 of former flue gases duct;

9) air-cooler be connected with the cold air inlet on P1 position;

10) the fresh water (FW) conveyance conduit be connected with the fresh water (FW) nozzle on P2 position, preferably, the other end of this fresh water (FW) conveyance conduit is connected to the ammonia-containing water basin in relieving haperacidity district, or the other end of this fresh water (FW) conveyance conduit separates a branch road and is connected to the ammonia-containing water basin in relieving haperacidity district; With

11) booster fan between P1 and P2 position.

Preferably, ammonia nozzle is provided with in the inlet plenum of the first adsorption tower and/or the second adsorption tower, spray ammonia pipe array (such as 106a and 106b) is arranged it is further preferred that be provided with in ammonia nozzle and the clearance space in the first adsorption tower and/or the second adsorption tower between each bed in the inlet plenum of the first adsorption tower and/or the second adsorption tower.Each branch road of (dilution) ammonia transfer pipeline is connected with these nozzles respectively.

Preferably, the first point for measuring temperature and the second point for measuring temperature are set respectively in the front-end and back-end of position P1, and the 3rd point for measuring temperature is set in the downstream of position P2, in the upstream of the gas approach of the first adsorption tower.

In general, above-mentioned first adsorption tower or the second adsorption tower are single tower list bed type or many beds type adsorption tower.

Preferably, a gas baffle door is set in the upstream of P1 position.

According to the 3rd embodiment of the present utility model, provide a kind of flue gas desulfurization and denitration method comprising the desulfuring and denitrifying apparatus of the two adsorption tower of series connection using above-mentioned first embodiment or the second embodiment, the method comprises the following steps:

I) step of flue gas temperature control or the step of flue gas temperature adjustment: pass into cold wind by the cold air inlet (P1 place) of the air inlet upstream at the first adsorption tower and/or regulated the temperature of flue gas by fresh water (FW) nozzle (P2 place) to spray technology water in former smoke conveying duct in former flue gas conveying flue, the flue-gas temperature entered in the first adsorption tower inlet plenum is made to be adjusted in the temperature range of regulation, such as at 100-160 DEG C, preferably at 110-150 DEG C, more preferably 120-145 DEG C of scope; With

II) desulfurization, denitrification step: above 1) after temperature control or the flue gas through overregulating temperature enter into the inlet plenum of the first adsorption tower, flow through one or more active carbon beds of the first adsorption tower (or reaction tower) in step successively, flue gas with adsorb from first active carbon that tower top adds and carry out cross-current type and contact, pollutant wherein contained by flue gas is (as oxysulfide, nitrogen oxide, dioxin etc.) removed by active carbon, neat stress enters into the discharge chamber of the first adsorption tower and discharges afterwards, the active carbon having adsorbed pollutant is then discharged bottom the first adsorption tower, and optionally (such as when the first adsorption tower and the second adsorption tower double tower parallel work-flow), the flue gas of discharging from the discharge chamber of the first adsorption tower to be introduced in via one-level flue in the inlet plenum of the second adsorption tower and to flow through one or more active carbon beds of the second adsorption tower successively, while aforesaid operations, by dilute former flue gas input channel neutralization that ammonia (such as via ammonia valve V4) passes into the first adsorption tower optionally (such as via the first ammonia valve V5) pass in the one-level flue of the second adsorption tower and be optionally passed in the first adsorption tower and/or the second adsorption tower, wherein dilute ammonia and obtained by a kind of ammonia and air mixing device (M) by ammonia and air.

That is, the flue gas (such as via one-level flue 102a) of discharging from the discharge chamber of the first adsorption tower is delivered to the inlet plenum (when the first adsorption tower and the second adsorption tower double tower parallel work-flow) of the second adsorption tower or is delivered to blowdown stack (when operating separately when the first adsorption tower).

Preferably, said method is further comprising the steps:

III) active carbon analyzing step: the active carbon adsorbing pollutant is transferred to the thermal treatment zone of a kind of active carbon Analytic Tower with the thermal treatment zone on top and the cooling zone of bottom from the bottom of the first adsorption tower and/or the second adsorption tower, allow active carbon carry out resolving, regenerating, and resolve, regenerate after active carbon be downward through cooling zone after discharge bottom desorber; Wherein: top nitrogen being passed into Analytic Tower in resolving, and the bottom optionally simultaneously nitrogen being passed into Analytic Tower via the second nitrogen pipeline; With, passing into nitrogen in Analytic Tower will comprise SO from thermal desorption on active carbon ₂and NH ₃take out of from the centre portion between the thermal treatment zone and cooling zone of desorber at interior gas pollutant and deliver to acid making system and relieving haperacidity district goes relieving haperacidity.The waste water containing ammonia is produced in relieving haperacidity district.Ammonia-containing water is such as stored in ammonia-containing water basin.

In general, in the application, active carbon desulfurization denitrating technique can realize single adsorption tower independent operating and two adsorption tower series operations (see accompanying drawing 1).

In general, two adsorption towers (i.e. the first adsorption tower and the second adsorption tower) of series connection adopt one of following two kinds of modes to run:

Single adsorption tower (the first adsorption tower) independent operating: open the first baffle door and third gear plate door, closes second baffle door and fourth gear plate door; Former flue gas enters in the first adsorption tower through baffle door, is purified after fully contacting in the first adsorption tower with active carbon, the flue gas after purification through third gear plate gate open to smoke stack emission; And the active carbon having adsorbed pollutant in flue gas is discharged in the first adsorption tower, enter Analytic Tower through the 3rd active carbon conveyer and carry out activating and regenerating, active carbon after regeneration is after bolting, and bulky grain active carbon is delivered to the first adsorption tower Inner eycle through the first conveyer and used; Wherein, second ammonia valve closing, first ammonia valve opening, dilution ammonia to mix with former flue gas through the first ammonia valve or directly passes into (in the clearance space in such as inlet plenum and between each bed) in the first adsorption tower via the first ammonia valve.Second conveyor and the second adsorption tower suspend use.Such as, when the second adsorption tower normally stop transport or have an accident or fault time, adopt this operational mode.

Or

Two adsorption towers (the first adsorption tower and the second adsorption tower) series operation: open the first baffle door, second baffle door and fourth gear plate door, closes third gear plate door; Former flue gas enters in the first adsorption tower through the first baffle door, in the first adsorption tower, flue gas is able to Partial cleansing, the flue gas now flowed out from the first adsorption tower enters the second adsorption tower through second baffle door again and carries out deep purifying, the flue gas after purification through fourth gear plate gate open to smoke stack emission; And the active carbon having adsorbed pollutant in flue gas is discharged in the first adsorption tower, enter Analytic Tower through the 3rd active carbon conveyer and carry out activating and regenerating, active carbon after regeneration is after bolting, bulky grain active carbon is delivered in adsorption tower through the first conveyer, active carbon is expelled to the second active carbon conveyer participate in gas cleaning reaction in the second adsorption tower after, then deliver to the top of the first adsorption tower, so recycle; Wherein, dilution ammonia is mixed with former flue gas by the first ammonia valve, or is mixed in one-level flue with the Partial cleansing flue gas of discharging from the first adsorption tower by the second ammonia valve; Or dilution ammonia directly to pass in the first adsorption tower (in the clearance space in such as inlet plenum and between each bed) via the first ammonia valve and/or directly passes into (in the clearance space in such as inlet plenum and between each bed) in the second adsorption tower via the second ammonia valve.Ammonia use amount is relevant to pollutant levels in flue gas flow and flue gas.

Preferably, above-described I) step of flue gas temperature control or the step of flue gas temperature adjustment comprise following sub-step:

(1) first at the cold air inlet place of the upstream position P1 of the flue to the first activated carbon adsorber conveying high-temperature flue gas, by passing into cold air in this flue, first time cooling is carried out to flue gas,

(2) then spray in the flue gas in flue at the fresh water (FW) nozzle place of downstream position P2 of the position P1 passing into cold air as the cooling water of fresh water (FW) or cold mist to reduce the temperature of flue gas, to regulate the flue-gas temperature that enters the first adsorption tower at the T3 of setting _settingin scope, such as T3 _settingat 105-150 DEG C, preferably 115-145 DEG C of scope, flue gas continues to flow to adsorption tower along flue; With

(3) carry in flue to former flue gas and optionally in the flue gas in one-level flue, spray into dilution ammonia.

Preferably, in above step (1), arrange the first point for measuring temperature and the second point for measuring temperature respectively in the front side of position P1 and rear side, on-line measurement is in flue-gas temperature T1 in flue and T2 at these two points for measuring temperature, is wherein T2 in the desired value of the second point for measuring temperature or setting value _settingwherein T2 _settingit is value within the scope of 150-180 DEG C, preferably 160-170 DEG C;

When actual measurement T1 is higher than T2 _settingduring value, start above-mentioned sub-step (1) and (2): according to T1 and T2 _settingdifference carry out predicting and according to T2 and T2 _settingdifference carry out the flow that feedback carrys out cold wind in set-up procedure (1), to be regulated by T2 or to control at T2 _setting± a DEG C of scope, wherein a DEG C is at 2-10 DEG C; Or

When actual measurement T1 is lower than T2 _settingduring value, start above-mentioned sub-step (2), stop the operation of step (1), namely close cold wind valve, only carry out follow-up step (2); Or

When system malfunctions or orderly closedown, cut off the supply of flue gas, only operate above-mentioned sub-step (1), and stop the operation of sub-step (2), cold wind passed into the first adsorption tower and optionally pass in the second adsorption tower.

Preferably, according to T1-T2 _settingdifference △ T1, the flow of flue gas and the temperature of cold air calculate and determine the flow of the cold air in step (1), regulate the aperture of cold wind valve, thus flue-gas temperature T2 be reduced to T2 _setting± a DEG C of scope.

Preferably, in above step (2), in the downstream of position P2, in the upstream of the gas approach of the first adsorption tower, the 3rd point for measuring temperature is set, on-line measurement is in the temperature T3 of flue gas in flue at the 3rd point for measuring temperature, according to actual measurement T2 and the desired value at the 3rd point for measuring temperature place or preset value T3 _settingdifference carry out predicting and according to T3 and T3 _settingdifference carry out the flow that feeds back to adjust spray technology water, T3 is regulated or controls at T3 _setting± b DEG C of scope, wherein T3 _settingat 100-150 DEG C, preferably value within the scope of 110-145 DEG C, and wherein b DEG C be at 2-10 DEG C.

Generally, T2 _settingcompare T3 _settinghigh 20-50 DEG C, more preferably high 25-45 DEG C, more preferably high 30-40 DEG C.

Preferably, fresh water (FW) is or comprises the ammonia-containing water produced from relieving haperacidity district.Comprising SO ₂and NH ₃(gas) pollutant to be transported in relieving haperacidity district process after, obtain ammonia-containing water.By a part for ammonia-containing water alternative techniques water or alternative techniques water.So both can utilize the NH in waste water ₃, reduce and pass into pure NH in the first adsorption tower and/or the second adsorption tower ₃the consumption of gas, to flue gas cool-down, can arrange outward without waste water again.

Preferably, above-described air-ammonia mixing arrangement (M) comprises air duct, ammonia pipeline, air spiral section, ammonia spiral section, mixing section and mixed gas outlet, wherein ammonia pipeline inserts (or extending into) air duct from the side of the larger air duct of diameter, then bending extend a segment distance L along air duct axis along airflow direction (it is such as the 20-80% of mixing arrangement total length, more preferably 35-65%, such as L=0.2-2 rice, preferred 0.3-1.5 rice), the latter end of ammonia pipeline is ammonia spiral section, ammonia spiral section comprises m the spirality ammonia passage separated by the m in ammonia pipeline spiral plate extending longitudinally, in addition, the air spiral section corresponding with ammonia spiral section comprises n the volute type air passage separated by the n in the space between ammonia pipeline and air duct spiral plate extending longitudinally, it is mixing section after the end of these two kinds of passages, the end of mixing section is mixed gas outlet, wherein: m=1-6 and n=1-8, contrary with the hand of spiral of ammonia spiral section with the hand of spiral of air spiral section.

In general, air spiral section and ammonia spiral section concentric.

Preferably, m=1-4, n=1-6, more preferably m=2 or 3, and/or n=2,3,4 or 5.

Preferably, described mixing arrangement M also comprises the first deflection plate and/or the second deflection plate that are arranged in mixing section.Or in mixing section, be provided with the first deflection plate and/or the second deflection plate.

Generally, the overall diameter of this ammonia pipeline is the 30-70% of the internal diameter of air duct, preferred 40-60%.

Preferably, the first deflection plate is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall; Be Circular plate structure with the second deflection plate, be placed within mixing duct, have gap between plectane excircle and mixing duct to allow mist pass through.

Preferably, the second deflection plate is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall; First deflection plate is Circular plate structure, is placed within mixing duct, has gap to allow mist pass through between plectane excircle and mixing duct.

Preferably, the length of air spiral section is 0.7-2.8 times of the length of ammonia spiral section, and doubly, more preferably 1-2.0 doubly for preferred 0.8-2.5, and more preferably 1.2-1.8 doubly.

In addition, the length of mixing section is 0.4-1 times of the length of air spiral section, and preferred 0.6-0.8 doubly.

Preferably, the first deflection plate and the second deflection plate repeat to arrange 2 to 3 groups as one group.Or the first deflection plate and the second deflection plate are arranged alternately and arrange 1-3 respectively separately, preferably arrange 2 respectively separately.

Air spiral section and ammonia spiral section have the structure being similar to spring or virtual bomb spring.The volute type air passage of air spiral section or the spirality ammonia passage of ammonia spiral section pitch are separately 0.2-2:1 with the ratio (i.e. K/2R or k/2r) of screw diameter respectively, preferred 0.4-1.5:1, more preferably 0.6-1.0:1.

In the mixed process of air and ammonia, ammonia is passed into device M, then through ammonia spiral section from ammonia entrance.In ammonia spiral section porch, ammonia is divided into some parts, then along spiral tube runs, finally forms the ammonia air-flow of spiral in ammonia spiral section exit.Air is passed into the air duct of device from air intake, then through air spiral section.Be divided into some parts at air spiral section inlet air, then along spiral tube runs, finally form the air draught of spiral in air spiral section exit.At mixing section place, the ammonia air-flow of spiral and the air draught of reverse spiral form strong convective motion, can mix by very fast carrying out, and then mixed airflow is by the first deflection plate and the second deflection plate.Mixed airflow is become turbulent flow by the first deflection plate and the second deflection plate, continues the mixed effect strengthening air and ammonia, the mixed effect finally making air and ammonia reach desirable at mixed gas outlet place.

In addition, the first deflection plate and the second deflection plate repeat to arrange 2 to 3 groups as one group; Or first deflection plate and the second deflection plate be arranged alternately and arrange 1-3 respectively separately, preferably arrange 2 respectively separately.

Ammonia and air become rare ammonia after mixing in this mixing arrangement, are then passed in the exhaust gases passes before the gas approach of adsorption tower and in this adsorption tower.Described active carbon desulfurization denitrating system comprises activated carbon adsorber and Analytic Tower.

The diameter of ammonia pipeline and air duct depends on the size scale of adsorption tower.The size scale of adsorption tower is larger, and rare ammonia amount that needs pass into is larger, then the diameter of ammonia pipeline and air duct is larger.The overall diameter of ammonia pipeline is such as 5cm-80cm, and as 10-60cm, thickness of pipe wall is such as 1-2cm, as 1.5cm.The overall diameter of air duct is such as 10cm-120cm, and as 15-100cm, thickness of pipe wall is such as 1-2.5cm, as 1.5 or 2.0cm.The total length of ammonia-air mixing device M is 0.6-3.5 rice, preferred 1-3 rice, more preferably 1.5-2.5 rice.

Above-described air and ammonia mixing arrangement M are made up of air duct, ammonia pipeline, air spiral section, ammonia spiral section, mixing section and mixed gas outlet.Air is from air duct access equipment, and ammonia is from ammonia pipeline access equipment.Air duct size is greater than ammonia line size.Ammonia pipeline is inserted in air duct, then extends a segment distance (it is such as 20-80%, the more preferably 35-65% of mixing arrangement total length, such as L=0.2-2 rice, preferred 0.3-1.5 rice) along air duct axis along airflow direction.Being placed in the ammonia pipeline in air duct, the ammonia spiral section entrance along air duct axis starts to afterbody, belongs to ammonia spiral section.In ammonia spiral section, ammonia pipeline is divided into some parts, every part all extends back along axis spiral, until the outlet of ammonia spiral section, and spaced apart from each other with spiral plate between each part.Air spiral section belongs to a part for air duct, to air spiral section outlet end from air spiral section entrance.In air spiral section, annulus between ammonia pipeline and air duct is divided into some parts, every part all extends back along axis with the rotation direction spiral contrary with ammonia spiral pipeline section, until the outlet of air spiral section, and is spaced from each other with spiral plate between each part.Mixing section be positioned at air spiral section after immediately air spiral section, until a segment pipe of mixed gas outlet, its inside is provided with the first deflection plate, the second deflection plate, also can arrange the many groups deflection plate according to the first deflection plate and the second deflection plate sequential arrangement.Such as, the first deflection plate is Circular Plate structure, and Circular Plate cylindrical is connected with mixing duct inwall.Second deflection plate is Circular plate structure, is placed within mixing duct, has gap between plectane cylindrical and mixing duct, can hold mist and pass through.

Ammonia is mixed with the air that dilution air blasts by " ammonia blender ", make NH3 concentration lower than LEL, for preventing too low air temperature from condensing, need to heat mixed gas, the dilution ammonia after heating is evenly sprayed into by ammonia-spraying grid at adsorption column inlet flue.

Active carbon analytically top of tower is sent into, and discharges from tower bottom.In the bringing-up section on Analytic Tower top, the active carbon having adsorbed polluter is heated to more than 400 DEG C, and keeps more than 3 hours, the SO be tightly held by activated carbon ₂be released, generate " rich sulphur gas (SRG) ", SRG is delivered to relieving haperacidity workshop section and produces H ₂sO ₄.There is SCR or SNCR reaction in the NOX be tightly held by activated carbon, wherein bioxin major part is decomposed simultaneously.Analytic Tower is resolved institute's calorific requirement and is provided by a hot-blast stove, and blast furnace gas is after hot-blast stove combustion, and heat smoke sends into the shell side of Analytic Tower.Hot gas major part after heat exchange gets back to (another fraction is then outer drains into air) in hot air circulation blower, and the high temperature hot gas sending into hot-blast stove and new burning by it mixes.Be provided with cooling section in Analytic Tower bottom, blast air and the heat of active carbon is taken out of.Cooling section is provided with cooling blower, blasts cold wind and is cooled by active carbon, drains in air then.The tiny activated carbon granule and dust that are less than 1.2mm, through the screening of active carbon sieve, are removed, can be improved the adsorption capacity of active carbon by Analytic Tower active carbon out.It is the active carbon of high adsorption capacity that active carbon sieve shines upper thing, and activity is delivered to adsorption tower by 1# active carbon conveyer and recycles, and screenings then enters ash silo.Need in resolving to protect with nitrogen, the SO that nitrogen will parse as carrier simultaneously ₂take out of Deng pernicious gas.Nitrogen analytically passes into tower upper and lower, in the middle of Analytic Tower, collect discharge, simultaneously by SO adsorbed in active carbon ₂take out of, and deliver to acid making system and go relieving haperacidity.When nitrogen passes into above Analytic Tower, be heated to about 100 DEG C with nitrogen heater and pass into again in Analytic Tower.

The utility model mainly can produce a certain amount of containing NH for relieving haperacidity workshop section in active carbon desulfurization ₃waste water, although the amount of this waste water is not too many, NH ₃very high concentrations, deals with and bothers very much.The utility model can well address this problem, and does not only need to process this part ammonia-containing water, it effectively can also be utilized, kill two birds with one stone.

Here, the first adsorption tower of series connection and the second adsorption tower refer to: the neat stress outlet of the first adsorption tower is connected to the gas approach of the second adsorption tower via pipeline.

For design and the absorbing process thereof of flue gas (or waste gas) adsorption tower, a lot of document has been had to disclose in prior art, see such as US5932179, JP2004209332A, with JP3581090B2 (JP2002095930A) and JP3351658B2 (JPH08332347A), JP2005313035A.The application is no longer described in detail.

In the utility model, for adsorption tower, single tower list bed designs can be adopted, or the design of single-tower muiti-bed layer, such as inlet plenum (A)-desulphurized aetivated carbon bed (a)-denitration activity charcoal bed (b)-discharge chamber (B) or such as inlet plenum (A)-desulphurized aetivated carbon bed (a)-desulphurization denitration active carbon bed (b)-denitration activity charcoal bed (c)-discharge chamber (B).

In general, for the adsorption tower (1) in the utility model and (2) tower height independently of one another, such as 15-60 rice, preferred 20-50 rice, more preferably 25-45 rice.First reaction tower (1) and the second reaction tower (2) can adopt identical or different structure and size each other, preferably adopt identical structure and size.The tower height of adsorption tower refers to that active carbon exports to the height of adsorption tower top active carbon entrance bottom adsorption tower, i.e. the height of the agent structure of tower.

In the utility model, for the not special requirement of Analytic Tower, the Analytic Tower of prior art all can be used in the utility model.Preferably, Analytic Tower is the vertical Analytic Tower of shell pipe type, wherein active carbon inputs from tower top, flow through tube side downwards, then arrive at the bottom of tower, heated air then flows through shell side, and heated air enters from the side of tower, carry out heat exchange with the active carbon flowing through tube side and lower the temperature, then exporting from the opposite side of tower.In the utility model, for the not special requirement of Analytic Tower, the Analytic Tower of prior art all can be used in the utility model.Preferably, Analytic Tower is the vertical Analytic Tower of shell pipe type (or package type), wherein active carbon inputs from tower top, flow through the tube side of the thermal treatment zone, top downwards, then a cushion space be between the thermal treatment zone, top and cooling zone, bottom is arrived, then the tube side of cooling zone, bottom is flowed through, then arrive at the bottom of tower, heated air (or high-temperature hot-air) then flows through the shell side of the thermal treatment zone, the side of heated air (400-450 DEG C) the analytically thermal treatment zone of tower enters, carry out indirect heat exchange with the active carbon flowing through thermal treatment zone tube side and lower the temperature, then export from the opposite side of the thermal treatment zone of tower.The side of the cooling air analytically cooling zone of tower enters, and carries out indirect heat exchange with the active carbon of resolving, regenerating flowing through cooling zone tube side.After the indirect heat exchange, cooling air is warming up to 90-130 DEG C (according to appointment 100 DEG C).

In general, there is for the Analytic Tower in the utility model the tower height of 10-45 rice, preferably 15-40 rice, more preferably 20-35 rice usually.Desorber has 6-100 rice usually ², preferred 8-50 rice ², more preferably 10-30 rice ², further preferably 15-20 rice ²body cross-section amass.

For design and the regeneration method of active carbon of active carbon Analytic Tower, a lot of document has been had to disclose in prior art, JP3217627B2 (JPH08155299A) discloses a kind of Analytic Tower (i.e. desorber), it adopts double seal valve, logical noble gas sealing, screening, water-cooled.JP3485453B2 (JPH11104457A) discloses regenerator, can adopt preheating section, double seal valve, logical noble gas, Air flow or water-cooled.JPS59142824A discloses gas from cooling section for preheating active carbon.Chinese patent application 201210050541.6 (Shanghai Ke Liu company) discloses the scheme of the energy recycling of regenerator, which uses drier.JPS4918355B discloses and adopts blast furnace gas (blast furnace gas) to carry out regenerated carbon.JPH08323144A discloses the regenerator adopting fuel (heavy oil or light oil), uses air-heating furnace.China's utility model 201320075942.7 relates to heater and possesses the emission-control equipment of this heater (coal-fired, air heat).

Analytic Tower of the present utility model adopts air-cooled.

For the situation that Analytic Tower analytic ability is 10t active carbon per hour, traditional handicraft keeps the temperature coke-stove gas needed for 420 DEG C in Analytic Tower to be about 400Nm ³/ h, combustion air is about 2200Nm ³/ h, outer thermal wind exhausting is about 2500Nm ³/ h; Required cooling-air 30000Nm ³/ h, after cooling, active carbon temperature is 140 DEG C.

" parsing " and " regeneration " is in this application used interchangeably.

" optionally " expression is in this application carried out or is not carried out.

Advantage of the present utility model

1, can regulation activity charcoal contaminant removal capacity as required, improve equipment flexibility, adapt to the change of flue gas condition.

2, adopt series connection double tower, denitration rate significantly improves.

3, compared with traditional cooling technology, method and apparatus of the present utility model ensure that the security of system all the time, achieves the accurate control of the temperature of flue gas in adsorption tower (or reaction tower).The normal spray cooling adopted when running does not increase treatment quantity, the change of former smoke moisture or moisture fluctuation very little (< 1%) substantially, therefore on the low temperature active of active carbon almost without affecting.When system shutdown or fault, only need open cold blast sliding valve can conveniently control active carbon bed temperature.

4, by using a kind of special air-ammonia mixing arrangement, can allow the mixed effect that air and ammonia reach desirable, guarantee that ammonia enters in adsorption tower with suitable concentration, guarantee the safe operation of adsorption tower, save ammonia simultaneously, the efficiency of the desulphurization and denitration of adsorption tower can be improved, reduce equipment operation cost, and this device is easy and simple to handle, easily operate.

5, fully utilize the ammonia-containing water of the high concentration produced in the relieving haperacidity district (workshop section) of active carbon desulfurization system, both make use of the NH in waste water ₃, reduce the consumption being passed into ammonia in adsorption tower, to flue gas cool-down, can arrange outward without waste water again, the cost avoiding process waste water drops into.

Accompanying drawing explanation

Fig. 1 is the desulfuring and denitrifying apparatus comprising activated carbon adsorber and regenerating active carbon tower and the process flow diagram of prior art.

Fig. 2 A is the process flow diagram adopting the out of stock method of flue gas desulfurization of series connection double activated carbon adsorption tower of the present utility model.

Fig. 2 B is the flue-gas temperature Controlling Technology schematic flow sheet of activated carbon adsorber of the present utility model (single tower list bed type).

Fig. 3 of the present utility modelly comprises multiple (3) active carbon bed and implements the schematic diagram of single-tower muiti-bed stratotype adsorption tower of multistage spray ammonia.

Fig. 4 is the schematic diagram of the adsorption tower that the many beds of symmetrical expression double tower of the present utility model (having clearance space between each bed) design.

Fig. 5 is the schematic diagram of the adsorption tower that the many beds of symmetrical expression double tower of the present utility model (between each bed gapless space) design.

Reference numeral

1: adsorption tower or reaction tower; 101,101a, 101b, 101c, a, b, c, d, e: active carbon bed; 102: former flue gas or former flue gas conveying flue; 102a: one-level flue; 102b: secondary neat stress pipeline; 102c: three grades of neat stress pipelines; 103: neat stress; 104: active carbon input port; 104a: active carbon material feeding valve; 105: active carbon exports; 105b: active carbon blowdown valve; 106:(dilutes) ammonia; 106a, 106b: spray ammonia pipe array; 106c: air or hot-air; 106d: ammonia; 507: cold wind, 508: fresh water (FW) transfer pipeline; 509: cold blast sliding valve; 510: baffle door; 511: the first points for measuring temperature; 512: the second points for measuring temperature; 513: the three points for measuring temperature; 514: booster fan; 115, V1, V2, V3: ammonia valve; V4: the first ammonia valve; V5: the second ammonia valve; P1: cold air inlet; P2: fresh water (FW) nozzle (water jet); M: air/ammonia mixing arrangement.

1a: the second adsorption tower; 2: regenerator (or desorber); 309: chimney; 701: the first active carbon conveyers; 702: the second active carbon conveyers; 703: the three active carbon conveyers; 901: the first baffle doors; 902: second baffle door; 903: third gear plate door; 904: fourth gear plate door; 40: vibratory sieve.

A1: inlet plenum; B1: discharge chamber; H: adsorption section height.

A, b, c, d: active carbon layer

9: the hot blast of outer row; 10: the cold wind of outer row;

203: neat stress; 206: nitrogen;

301: bypass gas baffle; 302: former gas baffle; 303 flapper door seal blower fans; 304: sealing air heater; 305: ammonia dilution air; 306 ammonia blenders; 307: ammonia heater; 308: main chimney; 311: booster fan; 313: nitrogen heater; 314: from the flue gas of sintering machine; 315: dedust storehouse; 316: rich sulphur gas removes acid making system.

4: thermal circulation fan; 5: combustion fan; 5: heating furnace; 7: blast furnace gas; 8: cooling blower.

Fig. 6 is the schematic diagram of air of the present utility model/ammonia mixing arrangement M.

Fig. 7 is the partial schematic diagram of ammonia spiral section (610), wherein m=2.

Fig. 8 is the partial schematic diagram of ammonia spiral section (610) and air spiral section (609), wherein m=2, n=2.

Reference numeral

601, air intake; 602, air duct; 603, air duct spiral section entrance; 604, ammonia spiral pipeline section entrance; 605, ammonia entrance; 606, ammonia pipeline; 607, air spiral section spiral plate; 608, ammonia spiral section spiral plate; 609, air spiral section; 610, ammonia spiral section; 611, air duct spiral section outlet; 612, mixing section; 613, ammonia spiral pipeline section outlet; 614, the first deflection plate; 615, the second deflection plate; 616, mixed gas outlet; 617, mist.

A, B, C and D: be that the space between ammonia pipeline and air duct of air spiral section (609) is by spiral plate four parts spaced apart from each other (four subchannels).

E, F, G and H: be that the ammonia pipeline of ammonia spiral section (610) is by spiral plate four parts spaced apart from each other (four subchannels).

Detailed description of the invention

At all embodiments, SO in former flue gas ₂and NO _xcontent be respectively 800mg/Nm ³and 350mg/Nm ³.

The detailed description of the invention of the application is described below:

Mixing arrangement (M) used in the following embodiments comprises air duct (602), ammonia pipeline (606), air spiral section (609), ammonia spiral section (610), mixing section (612) and mixed gas outlet (616), wherein ammonia pipeline (606) inserts (or extending into) air duct from the side of the larger air duct (602) of diameter, then bending extend a segment distance L along air duct (602) axis along airflow direction (it is such as the 20-80% of mixing arrangement total length, more preferably 35-65%, such as L=0.2-2 rice, preferred 0.3-1.5 rice), the latter end of ammonia pipeline (606) is ammonia spiral section (610), ammonia spiral section (610) comprises m the spirality ammonia passage separated by the m in ammonia pipeline (606) spiral plate (608) extending longitudinally, in addition, the air spiral section (609) corresponding with ammonia spiral section (610) comprises n the volute type air passage separated by the n in the space between ammonia pipeline (606) and air duct spiral plate (607) extending longitudinally, it is mixing section (612) after the end of these two kinds of passages, the end of mixing section is mixed gas outlet (616), wherein: m=1-6 and n=1-8, preferably m=1-4 and n=1-6, it is further preferred that m=2 or 3, and n=2,3,4 or 5, the hand of spiral of air spiral section (609) is contrary with the hand of spiral of ammonia spiral section (610).

In general, air spiral section (609) and ammonia spiral section (610) concentric.

Preferably, m=1-4, n=1-6, more preferably m=2 or 3, and/or n=2,3,4 or 5.

Preferably, in mixing section, be provided with the first deflection plate (614) and/or the second deflection plate (615).Or the first deflection plate (614) and the second deflection plate (615) are as one group and repeat to arrange 2 to 3 groups; Or first deflection plate (614) and the second deflection plate (615) be arranged alternately and arrange 1-3 respectively separately, preferably arrange 2 respectively separately.

Generally, the overall diameter of this ammonia pipeline (606) is the 30-70% of the internal diameter of air duct (602), more preferably 40-60%.

Preferably, the first deflection plate (614) is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall; Second deflection plate (615) is Circular plate structure, is placed within mixing duct, has gap to allow mist pass through between plectane excircle and mixing duct.

Preferably, the second deflection plate (615) is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall; First deflection plate (614) is Circular plate structure, is placed within mixing duct, has gap to allow mist pass through between plectane excircle and mixing duct.

In general, the length of air spiral section (609) is 0.7-2.8 times of the length of ammonia spiral section (610), and doubly, more preferably 1-2.0 doubly for preferred 0.8-2.5, and more preferably 1.2-1.8 doubly.

In general, the length of mixing section (612) is 0.4-1 times of the length of air spiral section (609), and preferred 0.6-0.8 doubly.

Air spiral section and ammonia spiral section have the structure being similar to spring or virtual spring.The volute type air passage of air spiral section or the spirality ammonia passage of ammonia spiral section pitch are separately 0.2-2:1 with the ratio (i.e. K/2R or k/2r) of screw diameter respectively, preferred 0.4-1.5:1, more preferably 0.6-1.0:1.

Embodiment 1

Adopt Fig. 1 and Fig. 2 A and the flow process shown in Fig. 2 B.Wherein adsorption tower (1) and adsorption tower (1a) are as shown in Figure 2 A and 2 B, i.e. single tower list bed type adsorption tower.

Comprise a desulfuring and denitrifying apparatus for the two adsorption tower of series connection, it comprises

1) first adsorption tower (1) of connecting and the second adsorption tower (1a);

2) regenerating active carbon tower (2) (or Analytic Tower);

3) former flue gas conveying flue (102) of the upstream, flue gas input port of adsorption tower (1), this flue (102) is provided with cold air inlet (P1) and fresh water (FW) nozzle (P2),

4) one-level flue (102a), its front end is connected to the exhanst gas outlet of the first adsorption tower (1) and its rear end are connected to the second adsorption tower (1a) inlet plenum via second baffle door (902),

5) secondary neat stress pipeline (102b), its front end is connected to the exhanst gas outlet of the first adsorption tower (1) and its rear end is communicated to blowdown stack (308) via third gear plate door (10),

6) three grades of neat stress pipelines (102c), its front end is connected to the exhanst gas outlet of the second adsorption tower (1a) and its rear end is communicated to blowdown stack (308) via fourth gear plate door (904),

7) (dilution) ammonia transfer pipeline 106, wherein: on this pipeline 106, be provided with ammonia and air mixing device (M) (ammonia of the present utility model-air mixing device M as shown in Figure 6.M=4 and n=4.The overall diameter of ammonia pipeline is 33cm, and thickness of pipe wall is 1.5cm.The overall diameter of air duct is 55cm, and thickness of pipe wall is 2.0cm.The total length of ammonia-air mixing device M is 2.5 meters).Separate two ammonia branch roads from the latter end of this pipeline 106, these two branch roads are communicated to former flue gas conveying flue (102) and one-level flue (102a) respectively.

The flue (102) of its Central Plains flue gas is communicated to the air inlet of the first adsorption tower (1) via the first baffle door (901), the exhaust uptake of drawing from the gas outlet of adsorption tower (1) is divided into first (102a) (i.e. one-level flue) and second (102b) (i.e. secondary smoke pipeline), two branch roads, wherein the first branch road (102a) (i.e. one-level flue) is communicated to the air inlet of adsorption tower (1a) via second baffle door (902), second branch road (102b) (i.e. secondary smoke pipeline) is communicated to blowdown stack (308) via third gear plate door (10),

The exhaust uptake of drawing from the gas outlet of the second adsorption tower (1a) is communicated to above-mentioned blowdown stack (308) via fourth gear plate door (904),

The active carbon of discharging from the bottom of adsorption tower (1) is transported to the top of regenerator (2) by the 3rd (3#) active carbon conveyer (703), the thick activated carbon granule that the regenerated carbon of discharging from the bottom of regenerator (2) obtains after vibratory sieve (40) screening is transported to the top of adsorption tower (1) and/or adsorption tower (1a) by first (1#) active carbon conveyer (701), the active carbon of discharging from the bottom of adsorption tower (1a) is transported to the top of adsorption tower (1) by second (2#) active carbon conveyer (702).

8) cold air inlet (P1) be provided with on the upstream position P 1 of conveying flue (102), and the fresh water (FW) nozzle (P2) be provided with on the downstream position P2 of flue (102);

9) air-cooler (509) be connected with the cold air inlet (P1) on P1 position;

10) the fresh water (FW) conveyance conduit (508) be connected with the fresh water (FW) nozzle (P2) on P2 position, the branch road that the other end of this pipeline (508) separates is connected to the ammonia-containing water basin in relieving haperacidity district;

11) booster fan (514) between P1 and P2 position.

First point for measuring temperature and the second point for measuring temperature are set respectively in the front side of position P1 and rear side, and the 3rd point for measuring temperature is set in the downstream of position P2, in the upstream of the gas approach of the first adsorption tower (1).A gas baffle door (510) is set in the upstream of P1 position.

Adsorption tower (1) and (1a) have 1 active carbon bed respectively, as in figs. 2 a and 2b.In addition, in the inlet plenum of the first adsorption tower (1) and the second adsorption tower (1a), ammonia nozzle is provided with.

Adsorption tower (1) and (1a) have identical structure, structure and sizes different a little, and tower height is respectively 25 meters and 20 meters.From the flow 10 × 10 of the heat smoke of sintering machine ⁵nm ³/ h, humidity 8%.

The basic procedure of flue gas desulfurization and denitration method in activated carbon adsorber that present embodiment 1 a kind of comprises flue gas temperature control is as follows:

I) step of flue gas temperature control or the step of flue gas temperature adjustment, this step comprises following sub-step:

(1) first to the first activated carbon adsorber (1) conveying high-temperature flue gas flue upstream position P1 (namely, convert the site P1 of cold wind) cold air inlet place, by passing into cold air (namely converting cold wind) in this flue, first time cooling is carried out to flue gas

(2) then pass into cold air position P1 downstream position P2 (namely, water spray site P2) fresh water (FW) nozzle (P2) place in the flue gas in flue, spray into fresh water (FW) to reduce the temperature of flue gas, flue gas continues to flow to the first adsorption tower (1) along flue; With

(3) respectively to spraying into dilution ammonia (i.e. Dilution air ammonia in former flue gas conveying flue (102) and one-level flue (102a), 100 DEG C), slightly reduce the temperature (reducing about 1 DEG C) of two flue gas in flues.

II) desulfurization, denitrification step: above 1) after temperature control or the flue gas through overregulating temperature enter into the inlet plenum of the first adsorption tower (1), flow through the active carbon bed of adsorption tower (1) successively (as Fig. 1 and 2 A in step, shown in 2B), flue gas carries out cross-current type with the active carbon added from the first adsorption tower (1) top and contacts, pollutant wherein contained by flue gas is (as oxysulfide, nitrogen oxide, dioxin etc.) removed by active carbon, neat stress enters into discharge chamber and discharges afterwards, the active carbon having adsorbed pollutant is then discharged from adsorption tower (1) and (1a) bottom, and the flue gas of discharging from the discharge chamber of the first adsorption tower (1) to be introduced in the inlet plenum of the second adsorption tower (1a) via one-level flue (102a) and to flow through the active carbon bed of the second adsorption tower (1a) successively, while aforesaid operations, flue gas input channel (102) neutralization dilution ammonia being passed into the first adsorption tower (1) passes in the one-level flue (102a) of the second adsorption tower (1a) and is passed in the first adsorption tower (1) and the second adsorption tower (1a).Wherein diluting ammonia is obtained by above-mentioned ammonia and air mixing device (M) by ammonia and air.

In the operation of the method: open the first baffle door (901), second baffle door (902) and fourth gear plate door (904), close third gear plate door (903).Former flue gas enters in the first adsorption tower (1) through the first baffle door (901), in the first adsorption tower (1), flue gas is able to Partial cleansing, the flue gas now flowed out from the first adsorption tower (1) enters the second adsorption tower (1a) through second baffle door (902) again and carries out deep purification, and the flue gas after purification leads to chimney (308) discharge through fourth gear plate door (904).The active carbon having adsorbed pollutant in flue gas is discharged in the first adsorption tower (1); enter Analytic Tower (3) through the 3rd active carbon conveyer (703) and carry out activating and regenerating; active carbon after regeneration is after vibratory sieve (40) screening; bulky grain active carbon is delivered in the second adsorption tower (1a) through the first conveyer (701); active carbon is expelled to the second active carbon conveyer (702) participate in gas cleaning reaction in the second adsorption tower (1a) after; then deliver to the top of the first adsorption tower (1), so recycle.The dilution ammonia of 105 DEG C directly passes in the conveying flue (102) of the first adsorption tower (1) via the first ammonia valve V4, is directly passed in the conveying flue (102a) (i.e. one-level flue) of the second adsorption tower (1a) by the dilution ammonia of 105 DEG C via the second ammonia valve V5 simultaneously.

Be wherein T2 in the desired value of the second point for measuring temperature or setting value _setting=165 DEG C.On-line measurement is in the flue-gas temperature T1=344 DEG C in flue at the first point for measuring temperature of the front end of position P1.Because actual measurement T1 is higher than T2 _settingvalue, according to T1 and T2 _settingdifference carry out predicting and anticipation, due to T1 and T2 _settingdifference comparatively large, the result of prediction or anticipation significantly strengthens the flow of cold wind (significantly regulating) immediately; And then, after significantly regulating air quantity, on-line measurement is in the flue-gas temperature T2=185 DEG C in flue at the second point for measuring temperature of the rear end of position P1, accordingly according to T2 and T2 _settingdifference feed back, due to T1 and T2 _settingdifference less, therefore strengthen the flow (by a small margin regulate) of cold wind further by a small margin, until actual measurement T2 is conditioned or controls at T2 _setting(165) till within the scope of ± 5 DEG C, now, actual measurement T2 be stabilized in=about 165 DEG C, the technique water yield sprayed in flue is stabilized in 5.1m ³/ h.

Then, the 3rd point for measuring temperature place in the downstream of position P2, set by the upstream of the gas approach of adsorption tower (1), desired value herein or preset value T3 _settingbe set to 155 DEG C.According to actual measurement T2 (namely 165 DEG C) and the desired value at the 3rd point for measuring temperature place or preset value T3 _settingdifference carry out predicting and anticipation, because difference is slightly bigger than normal, therefore tune up by a small margin and spray the flow of cold water.Then, and then on-line measurement is in the temperature T3=150 DEG C of flue gas in flue at the 3rd point for measuring temperature, according to actual measurement T3 and T3 _settingdifference carry out feedback to finely tune the flow of spray technology water (pure water), T3 is controlled at T3 _setting(150 DEG C) ± 3 DEG C of scopes, after this, actual measurement T3 is stabilized in about 150 DEG C, and the humidity of flue gas is 8.75%.For spray ammonia leaves the leeway of cooling further.

Then, the ammonia of Dilution air is sprayed in the former flue gas flue (102) and one-level flue (102a) of adsorption tower (1) and (1a), slightly reduce the temperature of flue gas, the temperature of the flue gas entered in adsorption tower (1) and adsorption tower (1a) is kept relative stability respectively at about 145 DEG C and about 140 DEG C.

Record from the discharge chamber of adsorption tower (1a): the desulfurization degree of 98% and the denitration rate of 85%.

Embodiment 2

Adopt Fig. 1 and Fig. 2 A and the flow process shown in Fig. 2 B, but adsorption tower (1) and adsorption tower (1a) are as shown in Figure 3, i.e. single tower three bed type adsorption tower.

2) regenerating active carbon tower (2) (or Analytic Tower);

3) former flue gas conveying flue (102) of the upstream, flue gas input port of the first adsorption tower (1), this flue (102) is provided with cold air inlet (P1) and fresh water (FW) nozzle (P2),

5) secondary neat stress pipeline (102b), its front end is connected to the exhanst gas outlet of the first adsorption tower (1) and its rear end is communicated to blowdown stack (308) via third gear plate door (903),

7) (dilution) ammonia transfer pipeline 106, wherein: on this pipeline 106, be provided with ammonia and air mixing device (M) (ammonia of the present utility model-air mixing device M as shown in Figure 6.M=4 and n=4.The overall diameter of ammonia pipeline is 33cm, and thickness of pipe wall is 1.5cm.The overall diameter of air duct is 55cm, and thickness of pipe wall is 2.0cm.The total length of ammonia-air mixing device M is 2.5 meters).Separate 4 ammonia branch roads from the latter end of this pipeline 106, wherein 2 branch roads are communicated to former flue gas conveying flue (102) and one-level flue (102a) respectively.Other 2 branch roads are communicated to 2 sprays ammonia pipe array (106a and 106b) in the clearance space between 3 active carbon beds of adsorption tower (1).

The flue (102) of its Central Plains flue gas is communicated to the air inlet of the first adsorption tower (1) via the first baffle door (901), the exhaust uptake of drawing from the gas outlet of the first adsorption tower (1) is divided into first (102a) (i.e. one-level flue) and second (102b) (i.e. secondary smoke pipeline), two branch roads, wherein the first branch road (102a) (i.e. one-level flue) is communicated to the air inlet of the second adsorption tower (1a) via second baffle door (902), second branch road (102b) (i.e. secondary smoke pipeline) is communicated to blowdown stack (308) via third gear plate door (903),

The active carbon of discharging from the bottom of the first adsorption tower (1) is transported to the top of regenerator (2) by the 3rd (3#) active carbon conveyer (703), the thick activated carbon granule that the regenerated carbon of discharging from the bottom of regenerator (2) obtains after vibratory sieve (40) screening is transported to the top of the first adsorption tower (1) and/or the second adsorption tower (1a) by first (1#) active carbon conveyer (701), the active carbon of discharging from the bottom of the second adsorption tower (1a) is transported to the top of the first adsorption tower (1) by second (2#) active carbon conveyer (702).

9) air-cooler (509) be connected with the cold air inlet (P1) on P1 position;

11) booster fan (514) between P1 and P2 position.

Adsorption tower (1) and (1a) have 3 active carbon beds respectively, as shown in Figure 3.In addition, in the inlet plenum of adsorption tower (1) and (1a), be provided with ammonia nozzle, and be arranged spray ammonia pipe array (106a and 106b) in clearance space in adsorption tower (1) and (1a) between each bed.

First adsorption tower (1) and the second adsorption tower (1a) have identical structure, structure and sizes different a little, and tower height is respectively 25 meters and 20 meters.From the flow 10 × 10 of the heat smoke of sintering machine ⁵nm ³/ h, humidity 8%.

(1) first the upstream position P1 of the flue of high-temperature flue gas is carried (namely first to activated carbon adsorber (1), convert the site P1 of cold wind) cold air inlet (P1) place, by passing into cold air (namely converting cold wind) in this flue, first time cooling is carried out to flue gas

(3) respectively to spraying into dilution ammonia (i.e. Dilution air ammonia in former flue gas conveying flue (102) and one-level flue (102a), 100 DEG C), slightly reduce the temperature (reducing about 1 DEG C) of two flue gas in flues.Meanwhile, dilution ammonia is led to 2 sprays ammonia pipe array (106a and 106b) in the clearance space between 3 active carbon beds of adsorption tower (1).

II) desulfurization, denitrification step: above 1) after temperature control or the flue gas through overregulating temperature enter into the inlet plenum of adsorption tower (1), flow through three active carbon beds (as shown in Figure 3) of adsorption tower (1) in step successively, the active carbon that flue gas and the top from adsorption tower (1) add carries out cross-current type and contacts, pollutant wherein contained by flue gas is (as oxysulfide, nitrogen oxide, dioxin etc.) removed by active carbon, neat stress enters into discharge chamber and discharges afterwards, the active carbon having adsorbed pollutant is then discharged from adsorption tower (1) bottom, and the flue gas of discharging from the discharge chamber of the first adsorption tower (1) to be introduced in the inlet plenum of the second adsorption tower (1a) via one-level flue (102a) and to flow through the active carbon bed of the second adsorption tower (1a) successively, while aforesaid operations, flue gas input channel (102) neutralization dilution ammonia being passed into the first adsorption tower (1) passes in the flue (102a) (i.e. one-level flue) of the second adsorption tower (1a) and is passed in the first adsorption tower (1) and the second adsorption tower (1a).Wherein diluting ammonia is obtained by above-mentioned ammonia and air mixing device (M) by ammonia and air.

In the operation of the method: open the first baffle door (901), second baffle door (902) and fourth gear plate door (904), close third gear plate door (903).Former flue gas enters in the first adsorption tower (1) through the first baffle door (901), in the first adsorption tower (1), flue gas is able to Partial cleansing, the flue gas now flowed out from the first adsorption tower (1) enters the second adsorption tower (1a) through second baffle door (902) again and carries out deep purification, and the flue gas after purification leads to chimney (308) discharge through fourth gear plate door (904).The active carbon having adsorbed pollutant in flue gas is discharged in the first adsorption tower (1); enter Analytic Tower (2) through the 3rd active carbon conveyer (703) and carry out activating and regenerating; active carbon after regeneration is after vibratory sieve (40) screening; bulky grain active carbon is delivered in the second adsorption tower (1a) through the first conveyer (701); active carbon is expelled to the second active carbon conveyer (702) participate in gas cleaning reaction in the second adsorption tower (1a) after; then deliver to the top of the first adsorption tower (1), so recycle.The dilution ammonia of the first via directly passes into the flue (102) of the first adsorption tower (1) via the first ammonia valve V4, the dilution ammonia on the second tunnel directly passes into the flue (102a) (i.e. one-level flue) of the second adsorption tower (1a) via the second ammonia valve V5, meanwhile, the dilution ammonia on the 3rd road and the 4th tunnel is led to 2 sprays ammonia pipe array (106a and 106b) in the clearance space between 3 active carbon beds of the first adsorption tower (1).

Be wherein T2 in the desired value of the second point for measuring temperature or setting value _setting=165 DEG C.On-line measurement is in the flue-gas temperature T1=341 DEG C in flue at the first point for measuring temperature of the front end of position P1.Because actual measurement T1 is higher than T2 _settingvalue, according to T1 and T2 _settingdifference carry out predicting and anticipation, due to T1 and T2 _settingdifference comparatively large, the result of prediction or anticipation significantly strengthens the flow of cold wind (significantly regulating) immediately; And then, after significantly regulating air quantity, on-line measurement is in the flue-gas temperature T2=186 DEG C in flue at the second point for measuring temperature of the rear end of position P1, accordingly according to T2 and T2 _settingdifference feed back, due to T1 and T2 _settingdifference less, therefore strengthen the flow (by a small margin regulate) of cold wind further by a small margin, until actual measurement T2 is conditioned or controls at T2 _setting(165) till within the scope of ± 5 DEG C, now, actual measurement T2 be stabilized in=about 165 DEG C, the technique water yield sprayed in flue is stabilized in 5.2m ³/ h.

Then, the 3rd point for measuring temperature place in the downstream of position P2, set by the upstream of the gas approach of adsorption tower (1), desired value herein or preset value T3 _settingbe set to 155 DEG C.According to actual measurement T2 (namely 165 DEG C) and the desired value at the 3rd point for measuring temperature place or preset value T3 _settingdifference carry out predicting and anticipation, because difference is slightly bigger than normal, therefore tune up by a small margin and spray the flow of cold water.Then, and then on-line measurement is in the temperature T3=150 DEG C of flue gas in flue at the 3rd point for measuring temperature, according to actual measurement T3 and T3 _settingdifference carry out feedback to finely tune the flow of spray technology water (pure water), T3 is controlled at T3 _setting(150 DEG C) ± 3 DEG C of scopes, after this, actual measurement T3 is stabilized in about 150 DEG C, and the humidity of flue gas is 8.6%.For spray ammonia leaves the leeway of cooling further.

Then, the ammonia of Dilution air is sprayed in the former flue gas flue (102) in adsorption tower (1) and (1a) and one-level flue (102a), slightly reduce the temperature of flue gas, the temperature of the flue gas entered in adsorption tower (1) and (1a) is kept relative stability respectively at about 145 DEG C and about 140 DEG C.

Record from the discharge chamber of adsorption tower (1a): the desulfurization degree of 99.5% and the denitration rate of 95%.

Embodiment 3

Repeat above embodiment 2, just single reaction tower (1) independent operating.Record from the discharge chamber of adsorption tower (1): the desulfurization degree of 90% and the denitration rate of 40%.

Embodiment 4

When system is normally run, active carbon bed temperature 145 DEG C, exhaust gas volumn 1 × 10 ⁶nm ³/ h.Now system is normally stopped transport, and the operation of water spray and spray ammonia stops, cold blast sliding valve standard-sized sheet, and close former baffle board door of flue, booster fan normally runs, and now sucking cold blast rate is 2 × 10 ⁵nm ³after/h, 6h, active carbon bed temperature reduces to 75 DEG C, now can close booster fan.Whole system is shut-down operation safely.

Embodiment 5

Repeat embodiment 2, just use the ammonia of the present utility model-air mixing device M shown in Fig. 6.M=2 and n=2.The overall diameter of ammonia pipeline is 30cm, and thickness of pipe wall is 1.5cm.The overall diameter of air duct is 50cm, and thickness of pipe wall is 2.0cm.The total length of ammonia-air mixing device M is 2.1 meters.

The Homogeneous phase mixing of ammonia and air improves the utilization ratio of ammonia, guarantees the safe operation of adsorption tower, saves ammonia simultaneously, can improve the efficiency of the desulphurization and denitration of adsorption tower, reduce equipment operation cost, and this mixing arrangement is static mixer, easy and simple to handle.

Embodiment 6

Repeat embodiment 1, just use the ammonia of the present utility model-air mixing device M shown in Fig. 6.M=2 and n=2.The overall diameter of ammonia pipeline is 30cm, and thickness of pipe wall is 1.5cm.The overall diameter of air duct is 50cm, and thickness of pipe wall is 2.0cm.The total length of ammonia-air mixing device M is 2.1 meters.

Embodiment 7

Repeat embodiment 1, just in addition, using the part of the ammonia-containing water of generation in relieving haperacidity district (workshop section) as the fresh water (FW) be injected in flue gas, the fresh water (FW) of another part is pure water.

Both saved the pure water consumption of a part, and make use of again the ammonia of waste water, decrease the consumption of ammonia, and avoided the treatment and discharge problem of the ammonia-containing water that relieving haperacidity district produces simultaneously, save the cost of wastewater treatment.

Embodiment 8

Repeat embodiment 2, just in addition, using the part of the ammonia-containing water of generation in relieving haperacidity district (workshop section) as the fresh water (FW) be injected in flue gas, the fresh water (FW) of another part is pure water.

Embodiment 9

Repeat embodiment 2, just adsorption tower (1) and adsorption tower (1a) are as shown in Figure 4.

Embodiment 10

Repeat embodiment 2, just adsorption tower (1) and adsorption tower (1a) are as shown in Figure 5.

Claims

1. use the flue gas desulfurization and denitrification device of the two adsorption tower of series connection, it is characterized in that it comprises

1) first adsorption tower (1) of connecting and the second adsorption tower (1a),

2) regenerating active carbon tower or Analytic Tower (2),

3) former flue gas conveying flue (102) of the upstream, flue gas input port of the first adsorption tower (1), this flue (102) is provided with cold air inlet (P1) and/or fresh water (FW) nozzle (P2),

6) three grades of neat stress pipelines (102c), its front end is connected to the exhanst gas outlet of the second adsorption tower (1a) and its rear end is communicated to blowdown stack (308) via fourth gear plate door (904), and

7) ammonia transfer pipeline (106), wherein: on this pipeline (106), be provided with a kind of ammonia and air mixing device (M), the rear end of this pipeline (106) be communicated to former flue gas conveying flue (102) and one-level flue (102a) respectively and/or extend to the first adsorption tower (1) and the second adsorption tower (1a) interior and at the end of pipeline (106), ammonia nozzle has been installed, or separate multiple ammonia branch road from the latter end of this pipeline (106), these branch roads are communicated to former flue gas conveying flue (102) and one-level flue (102a) respectively and are optionally connected to multiple ammonia nozzle of the clearance space between one or more ammonia nozzle of the inlet plenum being arranged in the first adsorption tower (1) and the second adsorption tower (1a) and the optional each active carbon bed being positioned at the first adsorption tower (1) or the second adsorption tower (1a) or spray ammonia pipe array (as 106a and 106b),

The flue (102) of its Central Plains flue gas is communicated to the air inlet of the first adsorption tower (1) via the first baffle door (901), the exhaust uptake of drawing from the gas outlet of the first adsorption tower (1) is divided into the first branch road (i.e. one-level flue, 102a) He the second branch road (i.e. secondary smoke pipeline, 102b) two branch roads, wherein the first branch road (102a) is communicated to the air inlet of the second adsorption tower (1a) via second baffle door (902), second branch road (102b) is communicated to blowdown stack (308) via third gear plate door (10),

2. the flue gas desulfurization and denitrification device using the two adsorption tower of series connection according to claim 1, is characterized in that the first adsorption tower (1) and the second adsorption tower (1a) have one or more active carbon bed respectively; And/or

First adsorption tower (1) and the second adsorption tower (1a) have identical or different structure and size each other.

3. use the flue gas desulfurization and denitrification device of the two adsorption tower of series connection, it is characterized in that it comprises

2) regenerating active carbon tower (2) (or Analytic Tower),

3) former flue gas conveying flue (102) of the upstream, flue gas input port of the first adsorption tower (1),

The flue (102) of its Central Plains flue gas is communicated to the air inlet of the first adsorption tower (1) via the first baffle door (901), the exhaust uptake of drawing from the gas outlet of the first adsorption tower (1) is divided into the first branch road (102a) and the second branch road (102b) two branch roads, wherein the first branch road (102a) is communicated to the air inlet of the second adsorption tower (1a) via second baffle door (902), second branch road (102b) is communicated to blowdown stack (308) via third gear plate door (903)

The active carbon of discharging from the bottom of the first adsorption tower (1) is transported to the top of regenerator (2) by the 3rd (3#) active carbon conveyer (703), the thick activated carbon granule that the regenerated carbon of discharging from the bottom of regenerator (2) obtains after vibratory sieve (40) screening is transported to the top of the first adsorption tower (1) and/or the second adsorption tower (1a) by first (1#) active carbon conveyer (701), the active carbon of discharging from the bottom of the second adsorption tower (1a) is transported to the top of the first adsorption tower (1) by second (2#) active carbon conveyer (702),

8) cold air inlet be provided with on the upstream position (P1) of former flue gas conveying flue (102), and the fresh water (FW) nozzle be provided with on the downstream position (P2) of former flue gas conveying flue (102);

9) the optional air-cooler (509) be connected with the cold air inlet on (P1) position;

10) the fresh water (FW) conveyance conduit (508) be connected with the fresh water (FW) nozzle on (P2) position; With

11) booster fan (514) between (P1) and (P2) position is positioned at.

4. the flue gas desulfurization and denitrification device using the two adsorption tower of series connection according to claim 3, is characterized in that the first adsorption tower (1) and the second adsorption tower (1a) have one or more active carbon bed respectively; And/or

5. according to the flue gas desulfurization and denitrification device of the two adsorption tower of use series connection described in claim 1 or 3, it is characterized in that: this mixing arrangement (M) comprises air duct (602), ammonia pipeline (606), air spiral section (609), ammonia spiral section (610), mixing section (612) and mixed gas outlet (616), wherein ammonia pipeline (606) inserts air duct from the side of the larger air duct (602) of diameter, then bend and extend a segment distance L along air duct (602) axis along airflow direction, the latter end of ammonia pipeline (606) is ammonia spiral section (610), ammonia spiral section (610) comprises m the spirality ammonia passage separated by the m in ammonia pipeline (606) spiral plate (608) extending longitudinally, in addition, the air spiral section (609) corresponding with ammonia spiral section (610) comprises n the volute type air passage separated by the n in the space between ammonia pipeline (606) and air duct spiral plate (607) extending longitudinally, it is mixing section (612) after the end of these two kinds of passages, the end of mixing section is mixed gas outlet (616), wherein: m=1-6 and n=1-8, the hand of spiral of air spiral section is contrary with the hand of spiral of ammonia spiral section.

6. the flue gas desulfurization and denitrification device using the two adsorption tower of series connection according to claim 5, is characterized in that: described mixing arrangement also comprises the first deflection plate (614) and/or the second deflection plate (615) that are arranged in mixing section; And/or

The overall diameter of this ammonia pipeline (606) is the 30-70% of the internal diameter of air duct (602).

7. the flue gas desulfurization and denitrification device using the two adsorption tower of series connection according to claim 6, it is characterized in that: the first deflection plate (614) is Circular Plate structure, the excircle of Circular Plate is connected with mixing duct inwall; Be Circular plate structure with the second deflection plate (615), be placed within mixing duct, have gap between plectane excircle and mixing duct to allow mist pass through; Or

Second deflection plate (615) is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall; First deflection plate (614) is Circular plate structure, is placed within mixing duct, has gap to allow mist pass through between plectane excircle and mixing duct.

8. the flue gas desulfurization and denitrification device using the two adsorption tower of series connection according to claim 5, is characterized in that: the length of air spiral section (609) is 0.8-2.5 times of the length of ammonia spiral section (610); And/or

The length of mixing section (612) is 0.4-1 times of the length of air spiral section (609); And/or

Air spiral section (609) or the respective pitch of ammonia spiral section (610) are 0.2-2:1 with the ratio of screw diameter.

9. the flue gas desulfurization and denitrification device using the two adsorption towers of series connection according to claim 6, is characterized in that: the first deflection plate (614) and the second deflection plate (615) are as one group and repeat to arrange 2 to 3 groups; Or,

First deflection plate (614) and the second deflection plate (615) are arranged alternately and arrange 1-3 respectively separately.

10. the flue gas desulfurization and denitrification device using the two adsorption tower of series connection according to claim 5, is characterized in that: the overall diameter of this ammonia pipeline (606) is the 40-60% of the internal diameter of air duct (602); And/or

The length of air spiral section (609) is 1-1.5 times of the length of ammonia spiral section (610); And/or

M=1-4 and n=1-6.