CN204502825U - For ammonia and the air mixing device of activated carbon adsorber - Google Patents
For ammonia and the air mixing device of activated carbon adsorber Download PDFInfo
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- CN204502825U CN204502825U CN201420735533.XU CN201420735533U CN204502825U CN 204502825 U CN204502825 U CN 204502825U CN 201420735533 U CN201420735533 U CN 201420735533U CN 204502825 U CN204502825 U CN 204502825U
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Abstract
Be provided for ammonia and the air mixing device of activated carbon adsorber, this device comprises air duct, ammonia pipeline, air spiral section, ammonia spiral section, mixing section and mixed gas outlet, wherein ammonia pipeline is inserted in the larger air duct of diameter, then a segment distance is extended along air duct axis along airflow direction, ammonia spiral section comprises the multiple spirality ammonia passages separated by multiple longitudinal spiral plate, and air spiral section comprises the multiple volute type air passages separated by multiple longitudinal spiral plate, it is mixing section after the end of these two passages.Ammonia and air become rare ammonia after mixing in this mixing section, are then passed in the exhaust gases passes before the gas approach of adsorption tower and in this adsorption tower.Active carbon desulfurization denitrating system comprises activated carbon adsorber and Analytic Tower.
Description
Technical field
The utility model relates to ammonia for activated carbon adsorber and air mixing device, that is, the device of ammonia Dilution air, belongs to sinter fume process field.
Background technology
Adsorption tower is in active carbon desulfurization denitrating system, for pernicious gas in charcoal absorption flue gas, impurity provide the device in place.Adsorption tower is a symmetrical structure, and centre is inlet plenum, and respectively there are three layers of active carbon layer inlet plenum both sides, respectively has a discharge chamber in the outside of active carbon layer, wherein adopts entrance shutter to separate between inlet plenum and active carbon bed.Sinter fume enters into adsorption tower via inlet plenum, then enters into active carbon layer again by entrance shutter, completes the desulphurization denitration of flue gas at active carbon layer.
In dry reactive charcoal desulfurizing and denitrifying process, need to use ammonia to participate in reaction.In the industrial production, ammonia is all generally provide with the form of liquefied ammonia.After liquid ammonia gasification, its ammonia purity is very high, as directly applied in production, both wastes, dangerous again.For this reason, after liquid ammonia gasification, high purity ammonia gas needs first and air mixes, and then is passed in dry desulfurization denitrating technique and applies.The mixture homogeneity of ammonia and air have impact on the utilization ratio of ammonia to a great extent, therefore, how to make ammonia and air fully mix, and is a urgent problem.The utility model provides a kind of desulphurization denitration ammonia mixing arrangement, solves this problem.
Utility model content
Desulphurization denitration ammonia mixing arrangement of the present utility model is 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 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.
According to first embodiment of the present utility model, be provided for ammonia and the air mixing device of activated carbon adsorber, this device 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 (belonging to air duct latter end or mixing arrangement latter end) mixing section after the end of these two kinds of passages, in addition end that is rear or mixing section is mixed gas outlet, wherein the hand of spiral of m=1-6, n=1-8 and wherein air spiral section is contrary with the hand of spiral of ammonia 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, in mixing section, be provided with the first deflection plate and/or the second deflection plate.Or the first deflection plate and the second deflection plate are as one group and repeat to arrange 2 to 3 groups; Or first deflection plate and the second deflection plate be arranged alternately and arrange 1-3 respectively separately, preferably arrange 2 respectively separately.
Generally, the overall diameter of this ammonia pipeline is the 30-70% of the internal diameter of air duct, more preferably 40-60%.
Preferably, the first deflection plate is Circular Plate structure, and the excircle of Circular Plate is connected with mixing duct inwall; Second 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 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.
In general, 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 general, the length of mixing section is 0.4-1 times of the length of air spiral section, 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.
Device of the present utility model operates in accordance with the following methods: 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 0.8-3 rice, more preferably 1.0-2.5 rice.
Effect of the present utility model
The mixed effect that the utility model can allow 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 operates.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of air of the present utility model/ammonia mixing arrangement M.
Fig. 2 is the partial schematic diagram of ammonia spiral section 610, wherein m=2.
Fig. 3 is the partial schematic diagram of ammonia spiral section 610 and air spiral section 609, wherein m=2, n=2.
Fig. 4 is the schematic diagram comprising multiple (3) active carbon bed and implement the single-tower muiti-bed stratotype adsorption tower of multistage spray ammonia.
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).
1 or 100: adsorption tower or reaction tower; 101,101a, 101b, 101c: 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: rare ammonia; 106a, 106b: spray ammonia pipe array; 106c: air (or hot-air); 106d: ammonia; 107: inlet plenum; 108: discharge chamber; 115, V1, V2 or V3: ammonia valve; M: air/ammonia mixing arrangement.
Fig. 5 is the process flow diagram of the active carbon Analytic Tower (resolution system) of heated nitrogen in nitrogen heat exchanger at least partially of the cooling air arranged outside the cooling zone of utilization of the present utility model analytically tower.
Fig. 6 is the flue-gas temperature Controlling Technology schematic flow sheet of activated carbon adsorber of the present utility model or reaction tower.
Fig. 7 is the schematic diagram comprising the flue gas processing device of desulphurization denitration tower and Analytic Tower of the present utility model.
Reference numeral
1: adsorption tower or reaction tower; 101,101a, 101b, 101c: 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: dilution 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 and V3: ammonia valve; P1: cold air inlet; P2: fresh water (FW) nozzle (water jet); M: air/ammonia mixing arrangement.
2: desorber; 15 or 213: active carbon entrance to be regenerated; 16 or 214: regenerated carbon exports;
201 or G2: from the cold wind of cooling blower, 202: the SO exported from desorber
2concentrated gas; 203 or G1: from the hot blast of hot air circulation blower; 204 or G1 ': the hot blast returning hot air circulation blower; 205 or G1 ': the hot blast of outer row; 206: as the nitrogen of carrier gas; 207 or G2 ': the cold wind of outer row;
200: nitrogen heat exchanger; 211: the thermal treatment zone or bringing-up section; 212: cooling zone or cooling section; L1-L4 and L7: gas piping.
L11: nitrogen pipeline, L12:SO
2the transfer pipeline (delivering to acid making system) of concentrated gas.
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.
Detailed description of the invention
In order to understand the utility model further, below in conjunction with embodiment, the utility model is described in further detail, but be not limitation of the utility model, be to be understood that, these describe just in order to further illustrate feature and advantage of the present utility model, instead of the restriction to the utility model claim.The equivalent replacement of all any this areas done according to the utility model disclosure, all belongs to protection domain of the present utility model.
See Fig. 1-3, according to a concrete embodiment of the present utility model, be provided for ammonia and the air mixing device of activated carbon adsorber, this device 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 (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 the total length of mixing arrangement M, 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 (belonging to air duct latter end or mixing arrangement latter end) mixing section 612 after the end of these two kinds of passages, mixed gas outlet 616 afterwards, wherein m=1-6, n=1-8.The volute type air passage of air spiral section 609 or the spirality ammonia passage of ammonia spiral section 610 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.
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.
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.
Device of the present utility model operates in accordance with the following methods: ammonia is passed into device M, then through ammonia spiral section 610 from ammonia entrance.In ammonia spiral section 610 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 602 of device, then through air spiral section 609 from air intake.Be divided into some parts at air spiral section 609 inlet air, then along spiral tube runs, finally form the air draught of spiral in air spiral section exit.At mixing section 612 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 614 and the second deflection plate 615 can repeat to arrange 2 to 3 groups as one group.Two groups, as 14,15,14,15.Three groups, as 14,15,14,15,14,15.Or the first deflection plate 614 and the second deflection plate 615 are arranged alternately and arrange 1-3 respectively separately, preferably arrange 2 respectively separately.
As shown in Figure 4, for the adsorption tower in the utility model be the single-tower muiti-bed stratotype adsorption tower comprising multiple (3) active carbon bed and implement multistage spray ammonia.The tower height of adsorption tower is 15-50 rice, preferred 20-40 rice, more preferably 25-30 rice.Tower height 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.
Application Example 1
SO in former flue gas
2and NO
xcontent be respectively about 800mg/Nm
3about 350mg/Nm
3.
Adopt Fig. 5, the flow process shown in 6 and 7.Wherein adsorption tower as shown in Figure 4.
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 P2 on the downstream position P2 of flue,
3) air-cooler 109 be connected with the cold air inlet on P1 position,
4) the fresh water (FW) conveyance conduit 108 be connected with the fresh water (FW) nozzle P2 on P2 position, separates from this pipeline the ammonia-containing water basin that a branch road is connected to relieving haperacidity district, to contain the waste water of ammonia to fresh water (FW) nozzle P2 from basin conveying,
5) booster fan 114 between P1 and P2 position,
6) ammonia transfer pipeline 106, wherein: on this pipeline 106, be provided with ammonia and air mixing device M (ammonia of the present utility model-air mixing device M as shown in Figure 6.M=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, ammonia pipeline enter in air duct after extended distance L or length L be 1.2 meters).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 separating multiple ammonia branch road from the latter end of this pipeline 106, these branch roads are communicated to the multiple ammonia nozzles in conveying flue 102 and the one or more ammonia nozzle be optionally connected in the inlet plenum of adsorption tower 1 and the optional clearance space between each active carbon bed of adsorption tower 1 respectively;
First point for measuring temperature and second point for measuring temperature are set respectively in the front side of position P1 and rear side, 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%.
With
7) desorber 2, it comprises: the thermal treatment zone 211 on top and the cooling zone 212 of bottom and the mesozone be positioned between the two, be positioned at tower top for inputting the import of active carbon to be regenerated and being positioned at the outlet of active carbon of the output regeneration at the bottom of tower; Described desorber has the tower height of 10-45 rice, preferably 15-40 rice, more preferably 20-35 rice;
8) for the thermal treatment zone 211 inputs the first pipeline L1 of heated air;
9) for cooling zone 212 inputs the cooling blower 8 of normal temperature air;
10) top to Analytic Tower passes into the nitrogen pipeline L11 of nitrogen and is arranged in the nitrogen heat exchanger 200 of nitrogen pipeline L11;
11) for discharging the 4th pipeline L4 of cooling air G2 ' from cooling zone 212, the front end of L4 is connected to the air outlet of cooling zone 212, and wherein the rear end of this pipeline L4 is connected to the entrance of the heating medium passage of nitrogen heat exchanger 200;
12) the SO2 concentrated gas fairlead L12 drawn from the centre portion between the thermal treatment zone 211 and cooling zone 212 of desorber, it is connected to relieving haperacidity district; With
13) the second nitrogen input pipe (attached not shown) of the optional bottom for nitrogen being passed into Analytic Tower.
First point for measuring temperature and second point for measuring temperature are set respectively in the front side of position P1 and rear side, 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 pass into cold air position P1 downstream position P2 (namely, water spray site P2) fresh water (FW) nozzle place in the flue gas in flue, spray into fresh water (FW) to reduce the temperature of flue gas, flue gas continues to flow to adsorption tower along flue, wherein using the ammonia-containing water that produces in relieving haperacidity district (workshop section) as fresh water (FW) or the part (fresh water (FW) of another part is pure water) as fresh water (FW), to regulate the flue-gas temperature that enters adsorption tower at the T3 of setting
settingin scope, such as T3
settingat 100-150 DEG C, preferably 110-145 DEG C of scope; 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) 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 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, 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,
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, set by upstream the 3rd point for measuring temperature place 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 145 DEG C.
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, in the thermal treatment zone of Analytic Tower, active carbon carries out indirect heat exchange with the hot blast G1 inputted as heated air and is heated or be warming up to active carbon resolution temperature Td, causes active carbon to carry out resolving, regenerating at this Td temperature; Simultaneously by cooling blower, the cold air inlet in normal temperature air or cooling air G2 analytically tower cooler district is passed in the cooling zone of Analytic Tower, carry out indirect heat exchange to cool active carbon with the active carbon moved down in cooling zone, analytically the cooling air outlet of the cooling zone of tower discharges cooling air or cooling-air G2 ' (it has 130 ± 25 DEG C, the preferably 130 DEG C ± temperature of 20 DEG C, more preferably 130 DEG C ± 15 DEG C); And resolve, regenerate after active carbon be downward through cooling zone after bottom desorber, discharge (top coarse grained active carbon being turned back to again adsorption tower after screening); Wherein: the top of Analytic Tower will be passed into via nitrogen heat exchanger (200) as the nitrogen of carrier gas in resolving, and optionally will pass into the bottom of Analytic Tower via the second nitrogen pipeline as the nitrogen of carrier gas simultaneously; 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, in acid making system, producing the waste water containing ammonia.The ammonia-containing water produced in relieving haperacidity district substitutes above-mentioned fresh water (FW) or substitutes a part (fresh water (FW) of another part is pure water) for above-mentioned fresh water (FW).
In addition, analytically a part (such as 12-25vol%) of the cooling air outlet of the cooling zone of the tower cooling air of discharging or cooling-air G2 ' (having the temperature of about 120 DEG C) is via outer row pipeline L4 or be transported in nitrogen heat exchanger 200 via first branch road of this outer row pipeline L4 and carry out indirect heat exchange to heat the nitrogen as carrier gas with nitrogen, such as be heated to 130 DEG C ± 20 DEG C (preferably 130 DEG C ± 15 DEG C, more preferably 130 DEG C ± 10 DEG C), then, the cold wind G2 ' after experiencing heat exchange is discharged.
For comprising the large desulfurization denitrification apparatus that tower height is the adsorption tower of 24.5 meters, the present embodiment adopts ammonia/air mixing device M as static mixer, 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 operates.
Claims (10)
1. for ammonia and the air mixing device of activated carbon adsorber, it is characterized in that this device 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.
2. ammonia according to claim 1 and air mixing device, is characterized in that m=1-4, n=1-6.
3. ammonia according to claim 1 and air mixing device, is characterized in that this device comprises: the first deflection plate (614) and/or the second deflection plate (615) that are arranged in mixing section.
4. ammonia according to claim 1 and air mixing device, is characterized in that the overall diameter of this ammonia pipeline (606) is the 30-70% of the internal diameter of air duct (602).
5. ammonia according to claim 4 and air mixing device, is characterized in that the overall diameter of this ammonia pipeline (606) is the 40-60% of the internal diameter of air duct (602).
6., according to the ammonia in claim 1-5 described in any one and air mixing device, 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; Second deflection plate (615) is Circular plate structure, is placed within mixing duct, has gap to allow mist pass through between plectane excircle and mixing duct.
7., according to the ammonia in claim 1-5 described in any one and air mixing device, it is characterized in that the second deflection plate (615) is Circular Plate structure, the excircle of Circular Plate is connected with mixing duct inwall; First deflection plate (614) is Circular plate structure, is placed within mixing duct, has gap to allow mist pass through between plectane excircle and mixing duct.
8. the ammonia according to any one of claim 1-5 and air mixing device, 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).
9. ammonia according to claim 8 and air mixing device, is characterized in that the length of air spiral section (609) is 1-2.0 times of the length of ammonia spiral section (610).
10. the ammonia according to any one of claim 1-5 and air mixing device, is characterized in that the length of mixing section (612) is 0.4-1 times of the length of air spiral section (609), and/or
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.
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| CN201420735533.XU CN204502825U (en) | 2014-11-27 | 2014-11-27 | For ammonia and the air mixing device of activated carbon adsorber |
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| CN201420735533.XU CN204502825U (en) | 2014-11-27 | 2014-11-27 | For ammonia and the air mixing device of activated carbon adsorber |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106237966A (en) * | 2016-08-23 | 2016-12-21 | 南京大学 | The reactor of aromatic aldehyde is produced for the oxidation of toluene class material |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106237966A (en) * | 2016-08-23 | 2016-12-21 | 南京大学 | The reactor of aromatic aldehyde is produced for the oxidation of toluene class material |
| CN106237966B (en) * | 2016-08-23 | 2018-11-09 | 南京大学 | The reactor of production aromatic aldehyde is aoxidized for toluene substance |
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