CN105688626A - A flue gas desulphurization denitration method including flue gas temperature control and a device therefor - Google Patents
A flue gas desulphurization denitration method including flue gas temperature control and a device therefor Download PDFInfo
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Abstract
A flue gas desulphurization denitration method including flue gas temperature control in an activated-carbon adsorption column and a device therefor are provided. The method includes I) a step of flue gas temperature control and II) a step of desulphurization and denitration, wherein the step of flue gas temperature control comprises (1) a step of subjecting flue gas to first time of cooling by feeding cold air into a flue conveying high-temperature flue gas to the activated-carbon adsorption column from a cold-air inlet at an upstream position (P1) of the flue, and (2) spraying cooling water or cold water mist into the flue gas in the flue from a process water spray nozzle at the downstream position (P2) of the position (P1) from which the cold air is fed, adjusting the temperature of the flue gas fed into the adsorption column to be in a preset range of T3, for example, the T3 ranges from 105-150 DEG C. The temperature of the flue gas fed into the adsorption column is controlled by mixing with the cold air and spraying water.
Description
Technical field
The present invention relates to the employing flue gas desulfurization of activated carbon adsorber, method of denitration, more specifically, the present invention relates to flue gas (sintering flue gas) to have employed in the upstream of activated carbon adsorber or front end spray cooling simultaneously and convert the measure of cold wind cooling and control the flue-gas temperature entering adsorption tower 100～150 DEG C of scopes, the method being preferably controlled in 120～140 DEG C of scopes, these belong to sintering fume treatment field。
Background technology
For the sintering device flue gas of industrial smoke, especially steel and iron industry, employing includes activated carbon adsorber and the large-scale dry desulfurization of Analytic Tower, denitrification apparatus and technique are more satisfactory。Activated 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 including activated carbon adsorber and Analytic Tower (or regenerator), activated carbon adsorber for including the pollutant of oxysulfide, nitrogen oxides and dioxin from sintering flue gas or waste gas (especially the sintering flue gas of the sintering machine of steel and iron industry) absorption, and Analytic Tower is for the hot recycling of activated carbon。
But, for highly arriving the desulphurization denitration tower of 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 100～160 DEG C, it is preferable that control at 120～150 DEG C。
On the one hand, in order to prevent the activated carbon in bed from burning, strict control active carbon bed temperature lower than 165 DEG C, be preferably shorter than 160 DEG C。This is because, although the burning-point of activated carbon is at about 430 DEG C, but the chemical reaction occurred at activated carbon surface is generally exothermic reaction, and containing inflammable, combustion-supporting material on a small quantity in the dust in flue gas, and activated carbon itself also carries inflammability dust secretly。Without the strict temperature controlled in adsorption tower, then the existence of these flammable material or inflammability dust causes potential safety hazard at any time, light then may result in activated carbon spontaneous combustion in adsorption tower tens meters high, serious then cause dust explosion, the appearance of both 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。After sintering the intensified blower fan pressurization of former flue gas, temperature is generally 90 DEG C-200 DEG C, is more generally between 100-180 DEG C, and it is high to sinter oxygen content in flue gas, in tower, after activated carbon surface oxidation, bed temperature can exceed 5-15 DEG C than input gas temperature, therefore to guarantee the safe operation of desulfuring and denitrifying apparatus, needing the flue-gas temperature to entering adsorption tower to be controlled, generally arranging alarm temperature is 150 DEG C。Additionally, before adsorption tower stoppage in transit, active carbon bed temperature in tower must be kept lower than 90 DEG C, now to need active carbon bed is cooled, therefore to guarantee safe stoppage in transit, also must active carbon bed temperature be controlled。
On the other hand, activated carbon flue gas purification system needs the strict flue-gas temperature controlling to enter adsorption tower be higher than or be not less than 100 DEG C, be preferably above or be not less than 110 DEG C time properly functioning。This is because, if flue-gas temperature is lower than 100 DEG C, then enter the temperature of water vapour contained in the sintering flue gas in bed close to dew point (or set point), very easily become water and react the acid becoming severe corrosive with oxysulfide, cause the heavy corrosion of device and seriously reduce the effect of denitration, denitration。
Traditional flue gas cool-down method is independent spray cooling in flue gas。This cooling means can effectively control active carbon bed temperature when system is properly functioning, but can cause that smoke moisture is too high for cooling before system shutdown, causes that activated carbon can adsorb a large amount of steam in flue gas, reduces activated carbon low-temperature denitration activity。
Generally, activated carbon method flue gases purification has the features such as desulphurization denitration rate is high, by-product resourcebility utilizes, activated carbon can be recycled, and the principle of its desulphurization denitration is as follows:
Surface SO at activated carbon2Oxidized absorption forms sulphuric acid, its reaction equation:
2SO2+O2+2H2O→2H2SO4
If spraying into a small amount of ammonia in flue gas, SO can be accelerated2Absorption, its reaction equation:
NH3+H2SO4→NH4HSO4
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+O2+4NH3→4N2+6H2O
In reaction tower, meanwhile there is also following side reaction:
2NH3+H2SO4→(NH4)2SO4
And SO2With NH3Reaction rate than NO and NH3Reaction rate faster, SO2Existence inhibit the carrying out of denitration reaction。It addition, the SO in flue gas3, HF and HCl also can and NH3Reaction, for denitration, these side reactions can considerably increase the consumption of ammonia, adds operating cost。
Summary of the invention
It is an object of the invention to provide the control method of a kind of active carbon bed temperature, it can be ensured that system realizes safely and effectively temperature and controls when running and stop transport, it is prevented that accident occurs。In the upstream of activated carbon adsorber or front end, flue gas (sintering flue gas) be have employed spray cooling simultaneously and convert the measure of cold wind cooling to control in adsorption tower the temperature of active carbon bed 100～160 DEG C of scopes, it is preferable that controlling the method 120～150 DEG C of scopes。
Flue gas temperature control method used in this application have employed simultaneously and flue gas carries out spray cooling and converts cold wind cooling。During adsorption tower normal operation, if active carbon bed temperature is higher than 150 DEG C, then the injection point arranged before utilizing adsorption tower, after booster fan, in former flue gas, spray into atomized water flue gas is lowered the temperature, thus reducing active carbon bed temperature。The amount of the fresh water (FW) sprayed is determined by exhaust gas volumn and flue-gas temperature。
Adsorption tower is normally stopped transport or (device needs to shut down because of fault or maintenance under accident conditions; or during water-cooling system fault); in order to reduce temperature in adsorption tower when 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 reducing active carbon bed temperature in adsorption tower。
It addition, the means of the present invention is also used in activated carbon adsorber many sites injection Dilution air ammonia, it for taking into account the effect of desulfurization and denitration simultaneously, on the other hand, also assists in adjustment and/or the control of temperature in adsorption tower on the one hand。It may also be said that as the preferred scheme of the present invention, adopt above means or the measure flue-gas temperature to control in adsorption tower, in order to adsorb under desirable flue-gas temperature。
According to the first embodiment of the present invention, it is provided that a kind of include the sintering flue gas desulfurization of flue gas temperature control, method of denitration, the method comprises the following steps:
I) step of the step of flue gas temperature control or flue gas homoiothermic, this step includes following sub-step:
(1) first at the cold air inlet place of the upstream position P1 of the flue carrying high-temperature flue gas to activated carbon adsorber, by passing into cold air in this flue, flue gas is carried out first time cooling,
(2) then in the flue gas in flue, the fresh water (FW) for cooling down sintering flue gas is sprayed at the fresh water (FW) nozzle place passing into the downstream position P2 of position P1 of cold air, i.e. cooling water or cold mist, in order to regulate the flue-gas temperature entering adsorption tower at the T3 setSetIn scope, for instance T3SetAt 105-150 DEG C, it is preferable that 115-145 DEG C of scope, more preferably in 120-140 DEG C of scope；
II) desulfurization, denitrification step: above 1) step flows successively through one or more active carbon beds of adsorption tower after temperature control or the flue gas through overregulating temperature enter in the inlet plenum of adsorption tower, flue gas carries out cross-current type with the activated carbon added from absorption tower top and contacts, simultaneously, the flue gas input channel neutralization that dilution ammonia passes into adsorption tower optionally passes in adsorption tower, the wherein pollutant contained by flue gas, namely oxysulfide is included, nitrogen oxides and dioxin are at interior pollutant, removed by activated carbon, neat stress enters in discharge chamber and discharges afterwards, the activated carbon having adsorbed pollutant is then discharged bottom adsorption tower；
III) activated carbon analyzing step: by adsorbed the activated carbon of pollutant transfer to from the bottom of adsorption tower the thermal treatment zone and the bottom with top cooling zone a kind of activated carbon Analytic Tower the thermal treatment zone, allow activated carbon carry out resolving, regenerating, and the activated carbon after resolving, regenerating is discharged after being downward through cooling zone bottom desorber；Wherein: in resolving, nitrogen is passed into the top of Analytic Tower, and optionally together nitrogen is passed into via the second nitrogen pipeline the bottom of Analytic Tower；With, pass into nitrogen in Analytic Tower by from activated carbon thermal desorption include SO2And NH3Acid making system is taken and delivered to centre portion between the interior gas pollutant thermal treatment zone and cooling zone from desorber out of and antacid district goes antacid。Antacid district produces the waste water containing ammonia。
Preferably, in above step (1), be respectively provided with the first point for measuring temperature and the second point for measuring temperature in the front side of position P1 and rear side, on-line measurement is in flue-gas temperature T1 and the T2 in flue at the two point for measuring temperature, is wherein T2 in the desired value of the second point for measuring temperature or setting valueSetWherein T2SetIt it is value within the scope of 150-180 DEG C, preferred 160-170 DEG C。
When actual measurement T1 is higher than T2SetDuring value, start above-mentioned sub-step (1) and (2): according to T1 and T2SetDifference be predicted and according to T2 and T2SetDifference carry out feedback and carry out the flow of cold wind in set-up procedure (1), in order to T2 is regulated or controls at T2Set± a DEG C of scope, wherein a DEG C is at 2-10 DEG C。
When actual measurement T1 is lower than T2SetDuring 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)。
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 is passed in adsorption tower。
Preferably, according to T1-T2SetDifference △ T1, the flow of flue gas and the temperature of cold air calculate and determine the flow of cold air in step (1), regulate the aperture of cold wind valve, thus flue-gas temperature T2 is reduced to T2Set± a DEG C of scope。
Further preferably, in above step (2), downstream at position P2, the gas approach at adsorption tower upstream the 3rd point for measuring temperature is set, the temperature T3 that on-line measurement is in flue flue gas 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 T3SetDifference be predicted and according to T3 and T3SetDifference carry out feeding back the flow adjusting spray technology water, by T3 regulate or control at T3Set± b DEG C of scope, wherein T3SetBe at 100-150 DEG C, it is preferable that 110-145 DEG C of scope, enclose interior value more preferably in 120-140 DEG C, and wherein b DEG C be at 2-10 DEG C。
Generally, T2SetCompare T3SetHigh 20-50 DEG C, more preferably high 25-45 DEG C, more preferably high 30-40 DEG C。
Preferably, fresh water (FW) is or includes the ammonia-containing water from antacid district。Comprising SO2And NH3(gas) pollutant be transported in antacid district process after, it is thus achieved that ammonia-containing water。A part by ammonia-containing water alternative techniques water or alternative techniques water。So both can utilize the NH in waste water3, reduce and pass into pure NH in adsorption tower3The consumption of gas, to flue gas cool-down, can arrange without outside waste water again。
It may further be preferable that in step (II), dilution ammonia (i.e. Dilution air ammonia) is obtained by air and ammonia mixing arrangement (M) with air by ammonia。
When adsorption tower is normally stopped transport or adsorbent equipment and/or water cooling plant have an accident, (such as device needs to shut down because of fault or maintenance; or during water-cooling system fault); stop step (2) water spray; cut off the supply of flue gas, only operating procedure (1) or startup step (1) (namely open cold blast sliding valve and pass into cold air in flue) simultaneously。Therefore reduce rapidly the temperature of flue gas, and then reduce rapidly active carbon bed temperature in adsorption tower。So that it is guaranteed that the safety of adsorption tower is stopped transport, it is to avoid the generation of security incident, and avoid the destruction to equipment and to the damage of activated carbon in adsorption tower bed。
Generally, in normal operation, (1) first pass through to conveying high-temperature flue gas flue in pass into cold air flue gas is carried out first time cooling, (2) then pass into the downstream in cold air site to flue gas sprays into fresh water (FW) (cooling water or cold mist) (such as injection flow rate should be controlled by so that the humidity of flue gas lower than 12wt%, be preferably shorter than 10wt%, more preferably less than 9wt%) reduce the temperature of flue gas。It addition, by spraying into dilution ammonia (i.e. Dilution air ammonia) in the flue gas entered in adsorption tower after entering in adsorption tower, also regulate the temperature of flue gas in adsorption tower in lower degree。
The flue-gas temperature T1 come when conveying is higher, namely higher than T2SetTime, if water spray reduces flue-gas temperature in relying on merely or be essentially relying on step (2), can cause that the humidity of flue gas is higher, impact subsequent adsorbtion operation in adsorption tower, now, the intake of cold air (as being in the air under ambient temperature) should be strengthened in above (1) step to reduce the temperature of flue gas, and the injection flow rate in step (2) keeps relative stability。Thus it is ensured that the humidity of flue gas in entrance adsorption tower and temperature is relative stable。
When the flue-gas temperature T1 that conveying comes is on the low side, namely lower than T2SetTime, then mainly or solely rely on and step (2) is sprayed cold water so that the temperature of flue gas is greatly lowered。So, the humidity remaining able to guarantee to enter the flue gas in adsorption tower is relative stable with temperature。
When adsorption tower is normally stopped transport or has an accident, (device needs to shut down because of fault or maintenance; or during water-cooling system fault); in order to reduce temperature in adsorption tower when not increasing tower humidity; stop step (2) water spray (namely closing fresh water (FW) cooling system); cut off the supply (closing by former gas baffle) of flue gas simultaneously; only operating procedure (1) or startup step (1) (namely open cold blast sliding valve and pass into cold air in flue); thus reducing rapidly the temperature of flue gas, and then reduce rapidly active carbon bed temperature in adsorption tower。So that it is guaranteed that the safety of adsorption tower is stopped transport, it is to avoid the generation of security incident, and avoid the destruction to equipment and to the damage of activated carbon in adsorption tower bed。
According to the second embodiment of the present invention, it is provided that desulphurization and denitration device or for the desulphurization and denitration device in above method, it includes
1) adsorption tower,
2) the former flue gas conveying flue in the upstream, flue gas input port of adsorption tower, is wherein provided with cold air inlet on the upstream position P1 of flue, and is provided with fresh water (FW) nozzle on the downstream position P2 of flue,
3) air-cooler being connected with the cold air inlet on P1 position,
4) the fresh water (FW) conveyance conduit being 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 antacid 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 antacid district
5) booster fan between P1 and P2 position,
6) ammonia conveyance conduit 106, wherein: on this ammonia conveyance conduit, (such as middle section position) is provided with a kind of ammonia and air mixing device (M), the rear end of this ammonia conveyance conduit is respectively communicated in former flue gas is carried flue and/or extended to adsorption tower and is mounted with ammonia nozzle at its end, or from the latter end of this ammonia conveyance conduit, separate multiple ammonia branch road, these branch roads are respectively communicated to the multiple ammonia nozzles in former flue gas conveying flue (102) and the one or more ammonia nozzles being optionally coupled in the inlet plenum of adsorption tower and the optional clearance space between each active carbon bed of adsorption tower, with
7) desorber, it includes the thermal treatment zone on top and the cooling zone of bottom and is positioned at mesozone between the two。
Preferably, the first point for measuring temperature and the second point for measuring temperature it are respectively provided with in the front-end and back-end of position P1。Preferably, in the downstream of position P2, the 3rd point for measuring temperature is set in the upstream of the gas approach of adsorption tower。
Above-described ammonia and air mixing device (M) are the ammonia for activated carbon adsorber and air mixing device, are used for obtaining dilution ammonia。
Preferably, above-described air-ammonia mixing arrangement (M) includes air line, ammonia pipeline, air spiral section, ammonia spiral section, mixing section and mixed gas outlet, wherein ammonia pipeline inserts (or extending into) air line from the side of the bigger air line of diameter, then bending extend a distance into L along air line 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 includes m the spiral type ammonia passage separated by the spiral lamina of m longitudinal extension in ammonia pipeline, in addition, the air spiral section corresponding with ammonia spiral section includes n the volute type air passage separated by the spiral lamina of n longitudinal extension in the space between ammonia pipeline and air line, it it is mixing section after the end of both 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 includes the first deflection plate and/or the second deflection plate that are arranged in mixing section。Or in mixing section, it is 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 line, it is preferable that 40-60%。
Preferably, the first deflection plate is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall；It is Circular plate structure with the second deflection plate, is placed within mixing duct have gap between plectane excircle and mixing duct and mix gas pass through to allow。
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 and mix gas pass through to allow 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, it is preferable that 0.8-2.5 times, more preferably 1-2.0 times, more preferably 1.2-1.8 times。
Additionally, the length of mixing section is 0.4-1 times of the length of air spiral section, it is preferable that 0.6-0.8 times。
Preferably, the first deflection plate and the second deflection plate as one group and repeat to arrange 2 to 3 groups。Or, the first deflection plate and the second deflection plate are arranged alternately and are each respectively provided with 1-3, it is preferable that be each respectively provided with 2。
Air spiral section and ammonia spiral section have the structure being similar to spring or virtual spring。The ratio (K/2R or k/2r) of the volute type air passage of air spiral section or the spiral type respective pitch of ammonia passage of ammonia spiral section and screw diameter is 0.2-2:1, it is preferable that 0.4-1.5:1, more preferably 0.6-1.0:1。
In the air mixed process with ammonia, ammonia is passed into device M from ammonia entrance, is then passed through ammonia spiral section。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 line of device from air intake, is then passed through air spiral section。It is divided into some parts at air spiral section inlet air, then along spiral tube runs, finally forms 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, it is possible to carrying out quickly mixes, and then mixed airflow passes through 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 to strengthen the mixed effect of air and ammonia, finally makes air and ammonia reach desirable mixed effect at mixed gas outlet place。
It addition, the first deflection plate and the second deflection plate as one group and repeat to arrange 2 to 3 groups；Or first deflection plate and the second deflection plate be arranged alternately and be each respectively provided with 1-3, it is preferable that be each respectively provided with 2。
Ammonia becomes rare ammonia after mixing in this mixing arrangement with air, is then passed into the exhaust gases passes before the gas approach of adsorption tower Nei and in this adsorption tower。Described active carbon desulfurization denitrating system includes activated carbon adsorber and Analytic Tower。
The diameter of ammonia pipeline and air line depends on the size scale of adsorption tower。The size scale of adsorption tower is more big, it is necessary to the rare ammonia amount passed into is more big, then the diameter of ammonia pipeline and air line is more big。The overall diameter of ammonia pipeline is such as 5cm-80cm, and such as 10-60cm, thickness of pipe wall is such as 1-2cm, such as 1.5cm。The overall diameter of air line is such as 10cm-120cm, and such as 15-100cm, thickness of pipe wall is such as 1-2.5cm, such as 1.5 or 2.0cm。The total length of ammonia-air mixing device M is 0.6-3.5 rice, it is preferable that 1-3 rice, more preferably 1.5-2.5 rice。
Above-described air and ammonia mixing arrangement are made up of air line, ammonia pipeline, air spiral section, ammonia spiral section, mixing section and mixed gas outlet。Air is from air line access equipment, and ammonia is from ammonia pipeline access equipment。Air line is sized larger than ammonia line size。Ammonia pipeline is inserted in air line, extends a distance into (it is such as the 20-80% of mixing arrangement total length, more preferably 35-65%, such as L=0.2-2 rice, it is preferable that 0.3-1.5 rice) then along air line axis along airflow direction。At the ammonia pipeline being placed in air line, the ammonia spiral section entrance along air line axis starts to afterbody, belongs to ammonia spiral section。In ammonia spiral section, ammonia pipeline being divided into some parts, every part extends back all along axis spiral, until the outlet of ammonia spiral section, and spaced apart from each other with spiral lamina between each part。Air spiral section belongs to a part for air line, starts to the outlet of air spiral section to terminate from air spiral section entrance。In air spiral section, annulus between ammonia pipeline and air line is divided into some parts, every part extends back with the rotation direction spiral contrary with ammonia spiral pipeline section all along axis, until the outlet of air spiral section, and be spaced from each other with spiral lamina between each part。Mixing section is in after air spiral section immediately air spiral section, until a segment pipe of mixed gas outlet, it is internally provided with the first deflection plate, the second deflection plate, it is possible to 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 mixing gas and pass through。
The air that ammonia is blasted with dilution air by " ammonia blender " mixes, and makes NH3Concentration is lower than LEL, and for preventing too low air temperature from condensing, it is necessary to mixed gas is heated, the dilution ammonia after heating is uniformly sprayed into by ammonia-spraying grid at adsorption column inlet flue。
Activated carbon analytically top of tower is sent into, and discharges from tower bottom。In the bringing-up section on Analytic Tower top, the activated carbon having adsorbed polluter is heated to more than 400 DEG C, and keeps more than 3 hours, the SO being tightly held by activated carbon2Being released, generate " rich sulfur gas (SRG) ", SRG is delivered to antacid workshop section and produces H2SO4。The NO being tightly held by activated carbonXSCR or SNCR reaction occurs, and wherein two English major parts are decomposed simultaneously。Analytic Tower resolves institute's calorific requirement and is provided by an air stove, and after blast furnace gas burns in air stove, heat smoke sends into the shell side of Analytic Tower。Steam major part after heat exchange returns to (another fraction is then outer drains into air) in hot air circulation blower, it send into the high temperature hot gas mixing of air stove and new burning。It is provided with cooling section in Analytic Tower bottom, blasts air and the heat of activated carbon is taken out of。Cooling section is provided with cooling blower, blasts cold wind and is cooled down by activated carbon, drains in air outside then。Tiny activated carbon granule less than 1.2mm and dust, through activated carbon sieve screening, are removed, can be improved the absorbability of activated carbon by Analytic Tower activated carbon out。It is the activated carbon of high adsorption capacity that activated carbon sieve shines upper thing, and activity is delivered to adsorption tower by 1# activated carbon conveyer and recycles, and siftage then enters ash silo。Resolving needs protect with nitrogen, the SO that nitrogen will parse simultaneously as carrier2Take out of etc. harmful gas。Nitrogen analytically passes into tower upper and lower, collects discharge in the middle of Analytic Tower, simultaneously by SO adsorbed in activated carbon2Take out of, and deliver to acid making system and go antacid。When nitrogen passes into above Analytic Tower, it is heated to about 100 DEG C with nitrogen heater and passes into again in Analytic Tower。
The present invention is primarily directed in active carbon desulfurization antacid workshop section and can produce a certain amount of containing NH3Waste water, although the amount of this waste water is not too many, but NH3Very high concentrations, deals with and bothers very much。The present invention can well solve this problem, not only need not process this part ammonia-containing water, moreover it is possible to it effectively utilized, kill two birds with one stone。
Design and absorbing process thereof for flue gas (or waste gas) adsorption tower, prior art there is a lot of document disclosed, referring to such as US5932179, JP2004209332A, with JP3581090B2 (JP2002095930A) and JP3351658B2 (JPH08332347A), JP2005313035A。The application is no longer described in detail。
In the present invention, for adsorption tower, single-tower muiti-bed layer can be adopted to design, for instance 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)；Or adopt the many bed designs of symmetrical expression double tower, such as discharge chamber (B)-denitration activity charcoal bed (c)-desulphurization denitration active carbon bed (b)-desulphurized aetivated carbon bed (a)-inlet plenum (A)-desulphurized aetivated carbon bed (a)-desulphurization denitration active carbon bed (b)-denitration activity charcoal bed (c)-discharge chamber (B), or discharge chamber (B)-active carbon bed (d)-active carbon bed (c)-active carbon bed (b)-active carbon bed (a)-inlet plenum (A)-active carbon bed (a)-active carbon bed (b)-active carbon bed (c)-active carbon bed (d)-discharge chamber (B), or discharge chamber (B)-active carbon bed (e)-active carbon bed (d)-active carbon bed (c)-active carbon bed (b)-active carbon bed (a)-inlet plenum (A)-active carbon bed (a)-active carbon bed (b)-active carbon bed (c)-active carbon bed (d)-active carbon bed (e)-discharge chamber (B)。
In general, the tower height for the adsorption tower in the present invention is, for instance 15-60 rice, it is preferable that 20-50 rice, more preferably 25-45 rice。The tower height of adsorption tower refers to that activated carbon exports to the height of adsorption tower top activated carbon entrance bottom adsorption tower, i.e. the height of the agent structure of tower。
In the present invention, for the not special requirement of Analytic Tower, the Analytic Tower of prior art can be used in the present invention。Preferably, Analytic Tower is the vertical Analytic Tower of shell pipe type, wherein activated carbon inputs from tower top, flow downwardly through tube side, then arriving 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 activated carbon flowing through tube side and lower the temperature, then export from the opposite side of tower。In the present invention, for the not special requirement of Analytic Tower, the Analytic Tower of prior art can be used in the present invention。Preferably, Analytic Tower is the vertical Analytic Tower of shell pipe type (or package type) or pipe type, wherein activated carbon inputs from tower top, flow downwardly through the tube side of the thermal treatment zone, top, then a cushion space being between the thermal treatment zone, top and cooling zone, bottom is arrived, then flow through the tube side of cooling zone, bottom, 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 the thermal treatment zone of heated air (400-450 DEG C) analytically tower enters, carry out indirect heat exchange with the activated 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 zone of cooling air analytically tower enters, and carries out indirect heat exchange with the activated carbon resolving, regenerating flowing through cooling zone tube side。After the indirect heat exchange, cooling air is warming up to 120 ± 20 DEG C (such as 100-130 DEG C, 120 DEG C according to appointment)。
In general, the tower height of 10-45 rice, preferred 15-40 rice, more preferably 20-35 rice it is generally of for the Analytic Tower in the present invention。Desorber is generally of 6-100 rice2, preferred 8-50 rice2, more preferably 10-30 rice2, it is preferred that 15-20 rice2Body cross-section amass。
Design and regeneration method of active carbon for activated carbon Analytic Tower, prior art there is a lot of document disclosed, JP3217627B2 (JPH08155299A) discloses a kind of Analytic Tower (i.e. desorber), it adopts double seal valve, logical noble gas seals, screening, water-cooled (Fig. 3 referring in this patent)。JP3485453B2 (JPH11104457A) discloses regenerator (referring to Figure 23 and 24), can adopt preheating section, double seal valve, logical noble gas, air cooling or water-cooled。JPS59142824A discloses the gas from cooling section for preheating activated carbon。Chinese patent application 201210050541.6 (Shanghai Ke Liu company) discloses the scheme of the energy recycling of regenerator, which uses exsiccator 2。JPS4918355B discloses the use of blast furnace gas (blastfurnacegas) and carrys out regenerated carbon。JPH08323144A discloses the use of the regenerator of fuel (heavy oil or light oil), uses air-heating furnace (referring to Fig. 2, the 11-air stove of this patent, 12-fuel supply system)。China's utility model 201320075942.7 relates to heater and possesses the emission-control equipment (coal-fired, air heating) of this heater, referring to the Fig. 2 in this utility model patent。
The Analytic Tower of the present invention adopts air-cooled。
For the situation that Analytic Tower analytic ability is 10t activated carbon per hour, traditional handicraft keeps the temperature coke-stove gas needed for 420 DEG C in Analytic Tower to be about 400Nm3/ h, combustion air is about 2200Nm3/ h, outer thermal wind exhausting is about 2500Nm3/ h；Required cooling air 30000Nm3/ h, after cooling, activated carbon temperature is 140 DEG C。
" parsing " and " regeneration " in this application is used interchangeably。
" optionally " expression carries out or does not carry out in this application。" optional " expression is with or without。Analytic Tower and regenerator are used interchangeably。Regeneration and parsing are used interchangeably。It addition, parsing and desorbing are identical concepts。" bringing-up section " and " thermal treatment zone " are identical concepts。" cooling section " and " cooling zone " are identical concepts。
Advantages of the present invention
1, compared with tradition cooling technology, methods and apparatus of the present invention has been always ensured that the safety of system, achieves the accurate control of the temperature of flue gas in adsorption tower (or reaction tower)。The spray cooling adopted time properly functioning does not substantially increase treatment quantity, and former smoke moisture changes or moisture fluctuation only small (< 1%), therefore on the low temperature active of activated carbon almost without impact。When system shutdown or fault, only need to open cold blast sliding valve can conveniently control active carbon bed temperature。
2, by using a kind of special air-ammonia mixing arrangement, air and ammonia can be allowed to reach desirable mixed effect, 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, it is easy to operation。
3, comprehensively utilize the ammonia-containing water of the high concentration produced in the antacid district (workshop section) of active carbon desulfurization system, both make use of the NH in waste water3, reduce the consumption being passed in adsorption tower ammonia, to flue gas cool-down, can arrange without outside waste water again, it is to avoid process the cost input of waste water。
Accompanying drawing explanation
Fig. 1 is the desulfuring and denitrifying apparatus including activated carbon adsorber and regenerating active carbon tower and the process flow diagram of prior art。
The flue-gas temperature that Fig. 2 A is the activated carbon adsorber of the present invention or reaction tower controls process flow diagram。
Fig. 2 B is the schematic diagram of the flue gas processing device including desulphurization denitration tower and Analytic Tower of the present invention。
Fig. 3 is including multiple (3) active carbon bed and implementing the schematic diagram that multistage sprays the single-tower muiti-bed stratotype adsorption tower of ammonia of the present invention。
Fig. 4 is the schematic diagram of the adsorption tower that the many beds of symmetrical expression double tower (having clearance space between each bed) of the present invention design。
Fig. 5 is the schematic diagram of the adsorption tower that the many beds of symmetrical expression double tower (between each bed gapless space) of the present invention design。
Accompanying drawing labelling
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；103: neat stress；104: activated carbon input port；104a: active carbon material feeding valve；105: activated carbon exports；105b: activated 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 or V3: ammonia valve；P1: cold air inlet；P2: fresh water (FW) nozzle (water jet)；M: air/ammonia mixing arrangement。
2: desorber；15: activated carbon entrance to be regenerated；16: regenerated carbon exports；
30: activated carbon feed bin；
40: activated carbon (AC) vibrosieve；401: dust；
701: the first activated carbon conveyers；702: the second activated carbon conveyers；
A: inlet plenum；B: discharge chamber；H: adsorption section height。
Fig. 6 is the schematic diagram of the air/ammonia mixing arrangement M of the present invention。
Fig. 7 is the partial schematic diagram of ammonia spiral section (610), wherein m=2。
Fig. 8 is ammonia spiral section (610) and the partial schematic diagram of air spiral section (609), wherein m=2, n=2。
Accompanying drawing labelling
601, air intake；602, air line；603, air line spiral section entrance；604, ammonia spiral pipeline section entrance；605, ammonia entrance；606, ammonia pipeline；607, air spiral section spiral lamina；608, ammonia spiral section spiral lamina；609, air spiral section；610, ammonia spiral section；611, air line 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, mixing gas。
A, B, C and D: be that the space between ammonia pipeline and air line of air spiral section (609) is by spiral lamina 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 lamina four parts spaced apart from each other (four subchannels)。
Detailed description of the invention
SO in all of embodiment, former flue gas2And NOxContent respectively about 800mg/Nm3About 350mg/Nm3。
The specific embodiment of the present invention is described below:
The mixing arrangement (M) used in the following embodiments includes air line 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 line from the side of the bigger air line 602 of diameter, then bending extend a distance into L along air line 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 includes m the spiral type ammonia passage separated by the spiral lamina 608 of m longitudinal extension in ammonia pipeline 606, in addition, the air spiral section 609 corresponding with ammonia spiral section 610 includes n the volute type air passage separated by the spiral lamina 607 of n longitudinal extension in the space between ammonia pipeline 606 and air line, it it is mixing section 612 after the end of both passages, the end of mixing section is mixed gas outlet 616；Wherein: m=1-6 and n=1-8, it is preferred that 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, it is 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 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 be each respectively provided with 1-3, it is preferable that be each respectively provided with 2。
Generally, the overall diameter of this ammonia pipeline 606 is the 30-70% of the internal diameter of air line 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 and mix gas pass through to allow 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 and mix gas pass through to allow 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, it is preferable that 0.8-2.5 times, more preferably 1-2.0 times, more preferably 1.2-1.8 times。
In general, the length of mixing section 612 is 0.4-1 times of the length of air spiral section 609, it is preferable that 0.6-0.8 times。
Air spiral section and ammonia spiral section have the structure being similar to spring or virtual spring。The ratio (i.e. K/2R or k/2r) of the volute type air passage of air spiral section or the spiral type respective pitch of ammonia passage of ammonia spiral section and screw diameter is 0.2-2:1 respectively, it is preferable that 0.4-1.5:1, more preferably 0.6-1.0:1。
Embodiment 1
Adopt the flow process shown in Fig. 1 and adsorption tower (as illustrated in fig. 1 and 2)。
Activated carbon adsorption tower apparatus includes
1) adsorption tower (1),
2) the former flue gas conveying flue 102 in the upstream, flue gas input port of adsorption tower, is wherein provided with cold air inlet on the upstream position P1 of flue, and is provided with fresh water (FW) nozzle on the downstream position P2 of flue,
3) air-cooler 509 being connected with the cold air inlet on P1 position,
4) the fresh water (FW) conveyance conduit 508 being connected with the fresh water (FW) nozzle on P2 position,
5) booster fan 514 between P1 and P2 position, and
6) ammonia conveyance conduit 106, is provided with ammonia and the air mixing device M (ammonia of the present invention as shown in Figure 6-air mixing device M on this pipeline 106。M=2 and n=2。The overall diameter of ammonia pipeline is 33cm, and thickness of pipe wall is 1.5cm。The overall diameter of air line is 55cm, and thickness of pipe wall is 2.0cm。The total length of ammonia-air mixing device M is 2.5 meters), the multiple ammonia branch roads separated from this pipeline 106, these branch roads are connected respectively to the one or more ammonia nozzles in the inlet plenum of adsorption tower and the multiple ammonia nozzles in the clearance space between each active carbon bed。
It is respectively provided with the first point for measuring temperature and the second point for measuring temperature in the front side of position P1 and rear side, and the upstream in the downstream at position P2, the gas approach at adsorption tower arranges the 3rd point for measuring temperature。One gas baffle door is set in the upstream of P1 position。
The tower height of adsorption tower is 24.5 meters。Flow 6.5 × 10 from the heat smoke of sintering machine5Nm3/ h, humidity 8.1%。
The basic procedure of flue gas desulfurization and denitration method in activated carbon adsorber that present embodiment 1 a kind of includes flue gas temperature control is as follows:
I) step of the step of flue gas temperature control or flue gas homoiothermic, this step includes following sub-step:
(1) first at the upstream position P1 of the flue to activated carbon adsorber conveying high-temperature flue gas (namely, convert the site P1 of cold wind) cold air inlet place, by passing into cold air (namely converting cold wind) in this flue, flue gas is carried out first time cooling
(2) then spraying into cold mist to reduce the temperature of flue gas at the fresh water (FW) nozzle place passing into the downstream position P2 of position P1 of cold air (that is, the site P2 of water spray) in the flue gas in flue, flue gas continues towards adsorption tower along flue；With
(3) then rear the spraying in the flue gas entered in adsorption tower in the inlet plenum entering adsorption tower dilutes ammonia (i.e. Dilution air ammonia)；
II) desulphurization and denitration step: above 1) step flows through an active carbon bed (as illustrated in fig. 1 and 2) of adsorption tower (or reaction tower) after temperature control or the flue gas through overregulating temperature enter in the inlet plenum of adsorption tower, flue gas carries out cross-current type with the activated carbon added from absorption tower top and contacts, wherein the pollutant (such as oxysulfide, nitrogen oxides, dioxin etc.) contained by flue gas are removed by activated carbon, neat stress enters in discharge chamber and discharges afterwards, and the activated carbon having adsorbed pollutant is then discharged bottom adsorption tower。
It is wherein T2 in the desired value of the second point for measuring temperature or setting valueSet=165 DEG C。The on-line measurement the first point for measuring temperature in the front end of position P1 is in flue-gas temperature T1=346 DEG C in flue。Owing to actual measurement T1 is higher than T2SetValue, according to T1 and T2SetDifference be predicted and anticipation, due to T1 and T2SetDifference bigger, it was predicted that or the result of anticipation is significantly to strengthen the flow of cold wind (significantly regulate) immediately；And then, after significantly regulating air quantity, the on-line measurement the second point for measuring temperature in the rear end of position P1 is in flue-gas temperature T2=186 DEG C in flue, accordingly according to T2 and T2SetDifference feed back, due to T2 and T2SetDifference 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 T2Set(165) till within the scope of ± 5 DEG C, now, actual measurement T2 is stabilized in=about 165 DEG C, and the technique water yield sprayed in flue is stable at 4.35m3/h。
Then, the downstream at position P2, the gas approach at adsorption tower the 3rd point for measuring temperature place set by upstream, desired value herein or preset value T3SetIt is set to 155 DEG C。According to actual measurement T2 (namely 165 DEG C) with the desired value at the 3rd point for measuring temperature place or preset value T3SetDifference be predicted and anticipation, owing to difference is slightly smaller, therefore by a small margin tune up injection cold water flow。Then, and then on-line measurement be in flue flue gas at the 3rd point for measuring temperature temperature T3=150 DEG C, according to actual measurement T3 and T3SetDifference carry out feedback to finely tune the flow of spray technology water (cold water), T3 is controlled at T3Set(150 DEG C) ± 3 DEG C of scopes, hereafter, actual measurement T3 is stable at about 150 DEG C, and the humidity of flue gas is 8.7%。
Then, in the flue gas entered in adsorption tower, spray the ammonia of Dilution air, slightly reduce the temperature of flue gas so that the temperature entering the flue gas in adsorption tower keeps relative stability at about 146 DEG C。
Embodiment 2
Repeat embodiment 1, simply adopt the adsorption tower shown in Fig. 3 to replace the adsorption tower shown in Fig. 1。The tower height of adsorption tower is 24.5 meters。Flow 6.5 × 10 from the heat smoke of sintering machine5Nm3/ h, humidity 8.1%。
Wherein flue-gas temperature in adsorption tower, be for three beds between two clearance spaces in flue-gas temperature average。
The temperature (or active carbon bed temperature) entering the flue gas in adsorption tower keeps relative stability at about 140 DEG C。
Embodiment 3
Repeat embodiment 1, simply adopt the adsorption tower shown in Fig. 4 to replace the adsorption tower shown in Fig. 1。The tower height of adsorption tower is 30 meters。Flow 12 × 10 from the heat smoke of sintering machine5Nm3/ h, humidity 8%。
Wherein flue-gas temperature in adsorption tower, be for bed between clearance space in flue-gas temperature average。
The temperature (or active carbon bed temperature) entering the flue gas in adsorption tower keeps relative stability at about 140 DEG C。
Embodiment 4
Repeat embodiment 1, simply adopt the adsorption tower shown in Fig. 5 to replace the adsorption tower shown in Fig. 1。The tower height of adsorption tower is 32 meters。Flow 10 × 10 from the heat smoke of sintering machine5Nm3/ h, humidity 8%。
Wherein flue-gas temperature in adsorption tower, is the flue-gas temperature in inlet plenum。
The temperature (or active carbon bed temperature) entering the flue gas in adsorption tower keeps relative stability at about 150 DEG C。
Embodiment 5
When system is properly functioning, active carbon bed temperature 145 DEG C, exhaust gas volumn 1 × 106Nm3/ h。Now system is normally stopped transport, and the operation of water spray and spray ammonia stops, and former baffle board door of flue closed by cold blast sliding valve standard-sized sheet, and booster fan is properly functioning, and now sucking cold blast rate is 2 × 105Nm3After/h, 6h, active carbon bed temperature reduces to 75 DEG C, now can close booster fan。Whole system stops operation safely。
Embodiment 6
Repeat embodiment 1, simply use the ammonia-air mixing device M of the present invention shown in Fig. 6。M=4 and n=4。The overall diameter of ammonia pipeline is 30cm, and thickness of pipe wall is 1.5cm。The overall diameter of air line 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, it is ensured that the safe operation of adsorption tower, saves ammonia simultaneously, can improve the efficiency of the desulphurization and denitration of adsorption tower, reduces equipment operation cost, and this mixing arrangement is static mixer, easy and simple to handle。
Embodiment 7
Repeat embodiment 6, simply it addition, using in antacid district (workshop section), the ammonia-containing water of generation is as a part for the fresh water (FW) being 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 process and the emission problem of the ammonia-containing water that antacid district produces simultaneously, save the cost of wastewater treatment。
Claims (18)
1. including the sintering flue gas desulfurization of flue gas temperature control, method of denitration, the method comprises the following steps:
I) step of the step of flue gas temperature control or flue gas homoiothermic, this step includes following sub-step:
(1) first at the cold air inlet place of the upstream position (P1) of the flue carrying high-temperature flue gas to activated carbon adsorber, by passing into cold air in this flue, flue gas is carried out first time cooling,
(2) then in the flue gas in flue, the fresh water (FW) for cooling down sintering flue gas is sprayed at the fresh water (FW) nozzle place passing into the downstream position (P2) of position (P1) of cold air, i.e. cooling water or cold mist, in order to regulate the flue-gas temperature entering adsorption tower at the T3 setSetIn scope, for instance T3SetAt 105-150 DEG C, it is preferable that 115-145 DEG C of scope；
II) desulfurization, denitrification step: above 1) step flows successively through one or more active carbon beds of adsorption tower after temperature control or the flue gas through overregulating temperature enter in the inlet plenum of adsorption tower, flue gas carries out cross-current type with the activated carbon added from absorption tower top and contacts, simultaneously, the flue gas input channel neutralization that dilution ammonia passes into adsorption tower optionally passes in adsorption tower, the wherein pollutant contained by flue gas, namely oxysulfide is included, nitrogen oxides and dioxin are at interior pollutant, removed by activated carbon, neat stress enters in discharge chamber and discharges afterwards, the activated carbon having adsorbed pollutant is then discharged bottom adsorption tower；
III) activated carbon analyzing step: by adsorbed the activated carbon of pollutant transfer to from the bottom of adsorption tower the thermal treatment zone and the bottom with top cooling zone a kind of activated carbon Analytic Tower the thermal treatment zone, allow activated carbon carry out resolving, regenerating, and the activated carbon after resolving, regenerating is discharged after being downward through cooling zone bottom desorber；Wherein: in resolving, nitrogen is passed into the top of Analytic Tower, and optionally together nitrogen is passed into via the second nitrogen pipeline the bottom of Analytic Tower；With, pass into nitrogen in Analytic Tower by from activated carbon thermal desorption include SO2And NH3Acid making system is taken and delivered to centre portion between the interior gas pollutant thermal treatment zone and cooling zone from desorber out of and antacid district goes antacid。
2. method according to claim 1, wherein in above step (1), the first point for measuring temperature and the second point for measuring temperature it is respectively provided with in the front side of position (P1) and rear side, on-line measurement is in flue-gas temperature T1 and the T2 in flue at the two point for measuring temperature, is wherein T2 in the desired value of the second point for measuring temperature or setting valueSetWherein T2SetIt it is value within the scope of 150-180 DEG C, preferred 160-170 DEG C；
When actual measurement T1 is higher than T2SetDuring value, start above-mentioned sub-step (1) and (2): according to T1 and T2SetDifference be predicted and according to T2 and T2SetDifference carry out feedback and carry out the flow of cold wind in set-up procedure (1), in order to T2 is regulated or controls at T2Set± a DEG C of scope, wherein a DEG C is at 2-10 DEG C；Or
When actual measurement T1 is lower than T2SetDuring 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 is passed in adsorption tower。
3. method according to claim 2, wherein according to T1-T2SetDifference △ T1, the flow of flue gas and the temperature of cold air calculate and determine the flow of cold air in step (1), regulate the aperture of cold wind valve, thus flue-gas temperature T2 is reduced to T2Set± a DEG C of scope。
4. according to the method in claim 2 or 3, wherein in above step (2), downstream at position (P2), the gas approach at adsorption tower upstream the 3rd point for measuring temperature is set, the temperature T3 that on-line measurement is in flue flue gas 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 T3SetDifference be predicted and according to T3 and T3SetDifference carry out feeding back the flow adjusting spray technology water, by T3 regulate or control at T3Set± b DEG C of scope, wherein T3SetAt 105-150 DEG C, it is preferable that value within the scope of 115-145 DEG C, and wherein b DEG C be at 2-10 DEG C。
5. method according to claim 4, wherein T2SetCompare T3SetHigh 20-50 DEG C, more preferably high 25-45 DEG C, more preferably high 30-40 DEG C。
6. the method in any of the one of claim 1-5, wherein fresh water (FW) is or includes the ammonia-containing water produced in antacid district。
7. the method in any of the one of claim 1-6, wherein in step (II), dilution ammonia (i.e. Dilution air ammonia) is obtained by air-ammonia mixing arrangement (M) with air by ammonia, this mixing arrangement (M) includes air line (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 line from the side of the bigger air line (602) of diameter, then bend and extend a distance into L along air line (602) axis along airflow direction, the latter end of ammonia pipeline (606) is ammonia spiral section (610), ammonia spiral section (610) includes m the spiral type ammonia passage separated by the spiral lamina (608) of m longitudinal extension in ammonia pipeline (606), in addition, the air spiral section (609) corresponding with ammonia spiral section (610) includes n the volute type air passage separated by the spiral lamina (607) of n longitudinal extension in the space between ammonia pipeline (606) and air line, it it is mixing section (612) after the end of both passages, the end of mixing section is mixed gas outlet (616)；Wherein: m=1-6 and n=1-8, it is preferred that 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 is contrary with the hand of spiral of ammonia spiral section。
8. method according to claim 7, it is characterised in that: described mixing arrangement also includes 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 line (602), it is preferable that 40-60%, and/or
The ratio (K/2R or k/2r) of the volute type air passage of air spiral section (609) or the spiral type respective pitch of ammonia passage of ammonia spiral section (610) and screw diameter is 0.2-2:1。
9. method according to claim 8, it is characterised in that: the first deflection plate (614) is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall；It is Circular plate structure with the second deflection plate (615), is placed within mixing duct have gap between plectane excircle and mixing duct and mix gas pass through to allow；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 and mix gas pass through to allow between plectane excircle and mixing duct。
10. the method according to claim 7-9, it is characterised in that: the length of air spiral section (609) is 0.8-2.5 times of the length of ammonia spiral section (610), preferred 1-1.5 times；And/or
The length of mixing section (12) is 0.4-1 times of the length of air spiral section (9)。
11. the method according to claim 7-9, it is characterised in that: the first deflection plate (614) and the second deflection plate (615) 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 are each respectively provided with 1-3, it is preferable that be each respectively provided with 2。
12. desulfurization and denitrification apparatus or for the desulfurization in the method for any one in above claim 1-11 and denitrification apparatus, it includes
1) adsorption tower (1), the tower height of adsorption tower is 15-60 rice, it is preferable that 20-50 rice, more preferably 25-45 rice；
2) former flue gas conveying flue (102) in the upstream, flue gas input port of adsorption tower, is wherein provided with cold air inlet on the upstream position (P1) of flue, and is provided with fresh water (FW) nozzle on the downstream position (P2) of flue,
3) air-cooler (509) being connected with the cold air inlet on (P1) position,
4) the fresh water (FW) conveyance conduit (508) being connected with the fresh water (FW) nozzle on (P2) position, it is preferred that the other end of this pipeline (508) is connected to the ammonia-containing water basin in antacid district,
5) booster fan (514) between (P1) and (P2) position it is positioned at,
6) 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) is respectively communicated to conveying flue (102) and/or extends in adsorption tower and be mounted with ammonia nozzle at its end, or from the latter end of this pipeline (106), separate multiple ammonia branch road, these branch roads be respectively communicated to conveying flue (102) and be optionally coupled to be arranged in adsorption tower (1) inlet plenum one or more ammonia nozzles and the optional each active carbon bed being positioned at adsorption tower (1) between multiple ammonia nozzles of clearance space；With
7) desorber (2), it includes the thermal treatment zone on top and the cooling zone of bottom and is positioned at mesozone between the two。
13. desulphurization and denitration device according to claim 12, wherein: be respectively provided with the first point for measuring temperature and the second point for measuring temperature in the front-end and back-end of position (P1)；Preferably, further in the downstream of position (P2), arrange the 3rd point for measuring temperature in the upstream of the gas approach of adsorption tower。
14. the desulfurization according to claim 12 or 13, denitrification apparatus, it is characterized in that this mixing arrangement (M) includes air line (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 line from the side of the bigger air line (602) of diameter, then bend and extend a distance into L along air line (602) axis along airflow direction, the latter end of ammonia pipeline (606) is ammonia spiral section (610), ammonia spiral section (610) includes m the spiral type ammonia passage separated by the spiral lamina (608) of m longitudinal extension in ammonia pipeline (606), in addition, the air spiral section (609) corresponding with ammonia spiral section (610) includes n the volute type air passage separated by the spiral lamina (607) of n longitudinal extension in the space between ammonia pipeline (606) and air line, it it is mixing section (612) after the end of both passages, the end of mixing section is mixed gas outlet (616)；Wherein: m=1-6 and n=1-8, it is preferred that 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 is contrary with the hand of spiral of ammonia spiral section。
15. desulphurization and denitration device according to claim 14, it is characterised in that: described mixing arrangement also includes 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 line (602), it is preferable that 40-60%；And/or
The ratio (K/2R or k/2r) of the volute type air passage of air spiral section (609) or the spiral type respective pitch of ammonia passage of ammonia spiral section (610) and screw diameter is 0.2-2:1。
16. desulphurization and denitration device according to claim 15, it is characterised in that: the first deflection plate (614) is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall；It is Circular plate structure with the second deflection plate (615), is placed within mixing duct have gap between plectane excircle and mixing duct and mix gas pass through to allow；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 and mix gas pass through to allow between plectane excircle and mixing duct。
17. the desulphurization and denitration device in any of the one of claim 14-16, it is characterised in that: the length of air spiral section (609) is 0.8-2.5 times of the length of ammonia spiral section (610), preferred 1-1.5 times；And/or
The length of mixing section (612) is 0.4-1 times of the length of air spiral section (609)。
18. the desulphurization and denitration device in any of the one of claim 14-16, it is characterised in that: the first deflection plate (614) and the second deflection plate (615) 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 are each respectively provided with 1-3, it is preferable that be each respectively provided with 2。
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