CN204502756U - Comprise the flue gas desulfurization and denitrification device of flue gas temperature control - Google Patents
Comprise the flue gas desulfurization and denitrification device of flue gas temperature control Download PDFInfo
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- CN204502756U CN204502756U CN201420736235.2U CN201420736235U CN204502756U CN 204502756 U CN204502756 U CN 204502756U CN 201420736235 U CN201420736235 U CN 201420736235U CN 204502756 U CN204502756 U CN 204502756U
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Abstract
Comprise the flue gas desulfurization and denitrification device of flue gas temperature control, this device comprises: 1) adsorption tower (1); 2) former flue gas conveying flue (102) of the upstream, flue gas input port of adsorption tower, wherein on the upstream position (P1) of flue, be provided with cold air inlet, and be provided with fresh water (FW) nozzle on the downstream position (P2) of flue; 3) air-cooler (509) be connected with the cold air inlet on (P1) position; 4) the fresh water (FW) conveyance conduit (508) be connected with the water jet on (P2) position; 5) booster fan (514) between (P1) and (P2) position is positioned at, and 6) the one or more ammonia nozzle in the inlet plenum of adsorption tower and the multiple ammonia nozzles in the optional clearance space between each active carbon bed; A point for measuring temperature (1) and a point for measuring temperature (2) are set respectively in the front-end and back-end of position (P1), and a point for measuring temperature (3) is set in the downstream of position (P2), in the upstream of the gas approach of adsorption tower (1).By converting cold wind in flue gas, water spray controls the flue-gas temperature that enters in adsorption tower.
Description
Technical field
The utility model relates to for the desulphurization and denitration device in flue gas desulfurization, method of denitration.More particularly, the utility model relates to 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 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.
But 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 100 ~ 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.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 90 DEG C-200 DEG C, to be more generally between 100-180 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 the flue-gas temperature entering adsorption tower, generally arranging alarm temperature is 150 DEG C.In addition, before adsorption tower is stopped transport, active carbon bed temperature in tower must be kept lower than 90 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 when active carbon flue gas purification system normally runs the strict flue-gas temperature controlling to enter adsorption tower higher than or be not less than 100 DEG C, preferably higher than or be not less than 110 DEG C.This is because, if flue-gas temperature is 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 independent 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 reaction 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 and NH
3reaction, for denitration, these side reactions can considerably increase the consumption of ammonia, add operating cost.
Utility model content
The purpose of this utility model is to provide 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 100 ~ 160 DEG C of scopes, preferably controls the method 120 ~ 150 DEG C of scopes.
Flue gas temperature control method 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 above means or measure to control the flue-gas temperature in adsorption tower, to adsorb under desirable flue-gas temperature.
According to first embodiment of the present utility model, provide a kind of sintering flue gas desulfurization, the method for denitration that comprise flue gas temperature control, the method comprises the following steps:
I) step of flue gas temperature control or the step of flue gas temperature adjustment, this step comprises following sub-step:
(1) first at the cold air inlet place of the upstream position P1 of the flue to 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 in the flue gas in flue, the fresh water (FW) for cooling sinter fume is sprayed at the fresh water (FW) nozzle place of downstream position P2 of the position P1 passing into cold air, i.e. cooling water or cold mist, to regulate the flue-gas temperature that enters adsorption tower at the T3 of setting
settingin scope, such as T3
settingat 105-150 DEG C, preferably 115-145 DEG C of scope, more preferably 120-140 DEG C of scope;
II) desulfurization, denitrification step: above 1) after temperature control or the flue gas through overregulating temperature enter into the inlet plenum of adsorption tower, flow through one or more active carbon beds of adsorption tower in step successively, flue gas carries out cross-current type contact with from adsorbing active carbon that tower top adds, simultaneously, flue gas input channel neutralization dilution ammonia being passed into adsorption tower optionally passes in adsorption tower, pollutant wherein contained by flue gas, namely oxysulfide is comprised, nitrogen oxide and dioxin are at interior pollutant, removed by active carbon, neat stress enters into discharge chamber and discharges afterwards, the active carbon having adsorbed pollutant is then discharged bottom adsorption tower,
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 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.
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.
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).
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-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.
Further preferably, in above step (2), the upstream of the downstream at position P2, the gas approach at adsorption tower arranges the 3rd point for measuring temperature, 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
settingbe at 100-150 DEG C, preferably 110-145 DEG C of scope, more preferably enclose interior value at 120-140 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 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 adsorption tower
3the consumption of gas, to flue gas cool-down, can arrange outward without waste water again.
Further preferably, in step (II), dilution ammonia (i.e. Dilution air ammonia) is obtained by air and ammonia mixing arrangement (M) by ammonia and air.
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 setting up procedure (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 active carbon bed temperature in adsorption tower rapidly.Thus guarantee that the safety of adsorption tower is stopped transport, avoid the generation of security incident, and avoid the destruction of equipment and the damage to active carbon in adsorption tower bed.
Generally, in normal operation, (1) first by passing into cold air in the flue to conveying high-temperature flue gas, first time cooling is carried out to flue gas, (2) then spray in flue gas in the downstream passing into cold air site fresh water (FW) (cooling water or cold mist) (such as injection flow rate should be controlled, make the humidity of flue gas lower than 12wt%, preferably lower than 10wt%, more preferably less than 9wt%) reduce the temperature of flue gas.In 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 compared with temperature low degree regulating flue gas in adsorption tower.
When the flue-gas temperature T1 transported is higher, namely higher than T2
settingtime, rely on if simple or mainly rely on water spray in step (2) and reduce flue-gas temperature, the humidity of flue gas can be caused higher, the subsequent adsorbtion operation of impact in adsorption tower, now, should strengthen the intake of cold air (as the air be under environment temperature) to reduce the temperature of flue gas in above (1) step, and the injection flow rate in step (2) keeps relative stability.Like this, the relatively stable of the humidity and temperature of the flue gas entered in adsorption tower is guaranteed.
When the flue-gas temperature T1 transported is on the low side, namely lower than T2
settingtime, then mainly or only rely on spray cold water in step (2) and significantly reduce the temperature of flue gas.Like this, the relatively stable of the humidity and temperature of the flue gas entered in adsorption tower can still be guaranteed.
When adsorption tower is normally stopped transport or is had an accident (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; 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 setting up procedure (1) (namely open cold blast sliding valve and pass into cold air in flue); thus reduce rapidly the temperature of flue gas, and then reduce active carbon bed temperature in adsorption tower rapidly.Thus guarantee that the safety of adsorption tower is stopped transport, avoid the generation of security incident, and avoid the destruction of equipment and the damage to active carbon in adsorption tower bed.
According to second embodiment of the present utility model, provide desulphurization and denitration device or for the desulphurization and denitration device in above method, it comprises
1) adsorption tower,
2) at the former flue gas conveying flue of the upstream, flue gas input port of adsorption tower, wherein on the upstream position P1 of flue, be provided with cold air inlet, and be provided with fresh water (FW) nozzle on the downstream position P2 of flue,
3) air-cooler be connected with the cold air inlet on P1 position,
4) 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
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 communicated to former flue gas conveying flue respectively and/or extends in adsorption tower and to have installed ammonia nozzle at its end, or separate multiple ammonia branch road from the latter end of this ammonia conveyance conduit, these branch roads are communicated to the multiple ammonia nozzles in former flue gas conveying flue (102) and the one or more ammonia nozzle be optionally connected in the inlet plenum of adsorption tower and the optional clearance space between each active carbon bed of adsorption tower respectively, with
7) desorber, the mesozone that it comprises the thermal treatment zone on top and the cooling zone of bottom and is positioned between the two.
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.Preferably, the 3rd point for measuring temperature is set in the downstream of position P2, in the upstream of the gas approach of adsorption tower.
Above-described ammonia and air mixing device (M) are ammonia for activated carbon adsorber and air mixing device, for obtaining dilution ammonia.
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 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 (K/2R or k/2r) of screw diameter, 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 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 ", makes NH
3concentration is lower than LEL, and 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.The NO be tightly held by activated carbon
xsCR or SNCR reaction occurs, and 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.
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 muiti-bed layer can be adopted to design, such as inlet plenum (A1)-desulphurized aetivated carbon bed (a)-denitration activity charcoal bed (b)-discharge chamber (B1) or such as inlet plenum (A1)-desulphurized aetivated carbon bed (a)-desulphurization denitration active carbon bed (b)-denitration activity charcoal bed (c)-discharge chamber (B1); or adopt the many bed designs of symmetrical expression double tower, such as discharge chamber (B1)-denitration activity charcoal bed (c)-desulphurization denitration active carbon bed (b)-desulphurized aetivated carbon bed (a)-inlet plenum (A1)-desulphurized aetivated carbon bed (a)-desulphurization denitration active carbon bed (b)-denitration activity charcoal bed (c)-discharge chamber (B1), or discharge chamber (B1)-active carbon bed (d)-active carbon bed (c)-active carbon bed (b)-active carbon bed (a)-inlet plenum (A1)-active carbon bed (a)-active carbon bed (b)-active carbon bed (c)-active carbon bed (d)-discharge chamber (B1), or discharge chamber (B1)-active carbon bed (e)-active carbon bed (d)-active carbon bed (c)-active carbon bed (b)-active carbon bed (a)-inlet plenum (A1)-active carbon bed (a)-active carbon bed (b)-active carbon bed (c)-active carbon bed (d)-active carbon bed (e)-discharge chamber (B1).
In general, the tower height for the adsorption tower in the utility model is, such as 15-60 rice, preferred 20-50 rice, more preferably 25-45 rice.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) or pipe 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 120 ± 20 DEG C (such as 100-130 DEG C, 120 DEG C according to appointment).
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 (Fig. 3 see in this patent).JP3485453B2 (JPH11104457A) discloses regenerator (see Figure 23 and 24), 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 2.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 (see Fig. 2 of this patent, 11-hot-blast stove, 12-fuel supply system).China's utility model 201320075942.7 relates to heater and possesses the emission-control equipment of this heater (coal-fired, air heat), see the Fig. 2 in this utility model patent.
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." optional " expression is with or without.Analytic Tower and regenerator are used interchangeably.Regeneration and parsing are used interchangeably.In addition, resolving with desorb is identical concept." bringing-up section " and " thermal treatment zone " are identical concepts." cooling section " and " cooling zone " are identical concepts.
Advantage of the present utility model
1, 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.
2, 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.
3, 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 flue-gas temperature Controlling Technology schematic flow sheet of activated carbon adsorber of the present utility model or reaction tower.
Fig. 2 B is the schematic diagram comprising the flue gas processing device of desulphurization denitration tower and Analytic Tower of the present utility model.
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; 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 or V3: ammonia valve; P1: cold air inlet; P2: fresh water (FW) nozzle (water jet); M: air/ammonia mixing arrangement.
2: desorber; 15: active carbon entrance to be regenerated; 16: regenerated carbon exports;
203: neat stress; 205: the hot blast of outer row; 206: as the nitrogen of carrier gas; 207: the cold wind of outer row.
30: active carbon feed bin;
40: active carbon (AC) vibratory sieve; 401: dust;
701: the first active carbon conveyers; 702: the second active carbon conveyers;
A1: inlet plenum; B1: discharge chamber; H: adsorption section height.
A, b, c, d: active carbon layer
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 about 800mg/Nm
3about 350mg/Nm
3.
Detailed description of the invention of the present utility model 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 30-70% of the internal diameter of air duct 602, more preferably 40-60%.
Preferably, the first deflection plate 614 is Circular Plate structures, and the excircle of Circular Plate is connected with mixing duct inwall; Second deflection plate 615 is Circular plate structures, 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 structures, and the excircle of Circular Plate is connected with mixing duct inwall; First deflection plate 614 is Circular plate structures, 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 the flow process shown in Fig. 1 and adsorption tower (as illustrated in fig. 1 and 2).
Charcoal absorption tower apparatus comprises
1) adsorption tower (1),
2) at the former flue gas conveying flue 102 of the upstream, flue gas input port of adsorption tower, wherein on the upstream position P1 of flue, be provided with cold air inlet, and be provided with fresh water (FW) nozzle on the downstream position P2 of flue,
3) air-cooler 509 be connected with the cold air inlet on P1 position,
4) the fresh water (FW) conveyance conduit 508 be 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, this pipeline 106 is provided with ammonia and air mixing device M (ammonia of the present utility model-air mixing device M as shown in Figure 6.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 duct is 55cm, and thickness of pipe wall is 2.0cm.The total length of ammonia-air mixing device M is 2.5 meters), from multiple ammonia branch roads that this pipeline 106 separates, these branch roads are connected respectively to the one or more ammonia nozzle in the inlet plenum of adsorption tower and the multiple ammonia nozzles in the clearance space between each active carbon bed.
In the front side of position P1 and rear side, the first point for measuring temperature and the second point for measuring temperature are set respectively, and the downstream at position P2, the gas approach at adsorption tower upstream the 3rd point for measuring temperature is set.A gas baffle door is set in the upstream of P1 position.
The tower height of adsorption tower is 24.5 meters.From the flow 6.5 × 10 of the heat smoke of sintering machine
5nm
3/ 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 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 activated carbon adsorber 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 in the flue gas in flue, spray into cold mist to reduce the temperature of flue gas at the fresh water (FW) nozzle place of downstream position P2 (that is, the site P2 of water spray) of the position P1 passing into cold air, flue gas continues to flow to adsorption tower along flue; With
(3) dilution ammonia (i.e. Dilution air ammonia) is sprayed in the rear flue gas to entering in adsorption tower then in the inlet plenum entering adsorption tower;
II) desulphurization and denitration step: above 1) after temperature control or the flue gas through overregulating temperature enter into the inlet plenum of adsorption tower, flow through an active carbon bed (as illustrated in fig. 1 and 2) of adsorption tower (or reaction tower) in step, flue gas carries out cross-current type contact with from adsorbing active carbon that tower top adds, pollutant (as oxysulfide, nitrogen oxide, dioxin etc.) wherein contained by flue gas is removed by active carbon, neat stress enters into discharge chamber and discharges afterwards, and the active carbon having adsorbed pollutant is then discharged bottom adsorption tower.
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=346 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 T2 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 4.35m
3/ h.
Then, the 3rd point for measuring temperature place set by the upstream of the downstream at position P2, the gas approach at adsorption tower, 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 little, 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 (cold 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 8.7%.
Then, in the flue gas entered in adsorption tower, spray the ammonia of Dilution air, slightly reduce the temperature of flue gas, the temperature of the flue gas entered in adsorption tower is kept relative stability at about 146 DEG C.
Embodiment 2
Repeat embodiment 1, just 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.From the flow 6.5 × 10 of the heat smoke of sintering machine
5nm
3/ 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, just 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.From the flow 12 × 10 of the heat smoke of sintering machine
5nm
3/ 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, just 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.From the flow 10 × 10 of the heat smoke of sintering machine
5nm
3/ 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 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 6
Repeat embodiment 1, just use the ammonia of the present utility model-air mixing device M 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 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 7
Repeat embodiment 6, 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.
Claims (10)
1. comprise the flue gas desulfurization and denitrification device of flue gas temperature control, it is characterized in that it comprises
1) adsorption tower (1),
2) former flue gas conveying flue (102) of the upstream, flue gas input port of adsorption tower, wherein on the upstream position (P1) of flue, be provided with cold air inlet, and be provided with fresh water (FW) nozzle on the downstream position (P2) of flue,
3) air-cooler (509) be connected with the cold air inlet on upstream position (P1) position of flue,
4) the fresh water (FW) conveyance conduit (508) be connected with the fresh water (FW) nozzle on downstream position (P2) position of flue,
5) booster fan (514) between the upstream position (P1) of flue and downstream position (P2) position of flue 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 communicated to conveying flue (102) respectively and/or extends in adsorption tower and to have installed ammonia nozzle at its end, or separate multiple ammonia branch road from the latter end of this pipeline (106), these branch roads are communicated to conveying flue (102) respectively and are optionally connected to multiple ammonia nozzles of the clearance space between one or more ammonia nozzle of the inlet plenum being arranged in adsorption tower (1) and the optional each active carbon bed being positioned at adsorption tower (1), with
7) desorber (2), the mesozone that it comprises the thermal treatment zone on top and the cooling zone of bottom and is positioned between the two.
2. the flue gas desulfurization and denitrification device comprising flue gas temperature control according to claim 1, it is characterized in that one end of pipeline (508) is connected with above-mentioned fresh water (FW) nozzle, the other end is connected to the ammonia-containing water basin in relieving haperacidity district.
3. according to the flue gas desulfurization and denitrification device comprising flue gas temperature control described in claim 1 or 2, it is characterized in that: in the front-end and back-end of the upstream position (P1) of flue, the first point for measuring temperature and the second point for measuring temperature are set respectively, and in the downstream of the downstream position (P2) of flue, arrange the 3rd point for measuring temperature in the upstream of the gas approach of adsorption tower.
4. according to the flue gas desulfurization and denitrification device comprising flue gas temperature control described in claim 1 or 2, 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.
5. the flue gas desulfurization and denitrification device comprising flue gas temperature control according to claim 4, 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); And/or
Air spiral section (609) or the respective pitch of ammonia spiral section (610) are 0.2-2:1 with the ratio (K/2R or k/2r) of screw diameter.
6. the flue gas desulfurization and denitrification device comprising flue gas temperature control according to claim 5, 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.
7. the flue gas desulfurization and denitrification device comprising flue gas temperature control according to claim 4, 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).
8. the flue gas desulfurization and denitrification device comprising flue gas temperature control according to claim 5, 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.
9. the flue gas desulfurization and denitrification device comprising flue gas temperature control according to claim 4, 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.
10. the flue gas desulfurization and denitrification device comprising flue gas temperature control according to claim 4, is characterized in that, m=2 or 3, and n=2,3,4 or 5.
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Cited By (1)
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|---|---|---|---|---|
| US11571655B2 (en) | 2016-12-29 | 2023-02-07 | Institute Of Process Engineering, Chinese Academy Of Sciences | Activated carbon adsorption tower and gas purification device |
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| US11571655B2 (en) | 2016-12-29 | 2023-02-07 | Institute Of Process Engineering, Chinese Academy Of Sciences | Activated carbon adsorption tower and gas purification device |
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