CN202962277U - Small air quantity constant temperature smoke denitrating device - Google Patents
Small air quantity constant temperature smoke denitrating device Download PDFInfo
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- CN202962277U CN202962277U CN 201220546214 CN201220546214U CN202962277U CN 202962277 U CN202962277 U CN 202962277U CN 201220546214 CN201220546214 CN 201220546214 CN 201220546214 U CN201220546214 U CN 201220546214U CN 202962277 U CN202962277 U CN 202962277U
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- anemostat
- ammonia
- spatters
- heat exchanger
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- 239000000779 smoke Substances 0.000 title abstract description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 101
- 238000001704 evaporation Methods 0.000 claims abstract description 7
- 238000005507 spraying Methods 0.000 claims abstract description 6
- 239000007921 spray Substances 0.000 claims description 61
- 239000003546 flue gas Substances 0.000 claims description 55
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 52
- 239000003054 catalyst Substances 0.000 claims description 24
- 210000003800 Pharynx Anatomy 0.000 claims description 18
- 238000009833 condensation Methods 0.000 claims description 16
- 230000005494 condensation Effects 0.000 claims description 16
- 238000009834 vaporization Methods 0.000 claims description 10
- 238000000034 method Methods 0.000 abstract description 6
- 238000002156 mixing Methods 0.000 abstract description 3
- 239000003595 mist Substances 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000007789 gas Substances 0.000 description 11
- 230000000694 effects Effects 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 229910002089 NOx Inorganic materials 0.000 description 7
- 239000003638 reducing agent Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 239000000571 coke Substances 0.000 description 5
- 230000003197 catalytic Effects 0.000 description 4
- 239000006185 dispersion Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- XSQUKJJJFZCRTK-UHFFFAOYSA-N urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 230000001133 acceleration Effects 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000000903 blocking Effects 0.000 description 1
- 230000003139 buffering Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000001351 cycling Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000003009 desulfurizing Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000010574 gas phase reaction Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 230000000414 obstructive Effects 0.000 description 1
- 210000000056 organs Anatomy 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000000630 rising Effects 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 230000001340 slower Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Abstract
The utility model discloses a small air quantity constant temperature smoke denitrating device which comprises an air inlet section, an ammonia spraying element, a heat exchanger, an electric heater, a denitrating reactor and a connecting flue from top to bottom. The heat exchanger comprises a condensing chamber and an evaporating chamber. The condensing chamber is arranged between the ammonia spraying element and the electric heater. The evaporating chamber is arranged outside the condensing chamber in parallel and is connected with the outlet of a smoke denitrating reactor through the connecting flue. The device provided by the utility model is particularly suitable for small air quantity constant temperature smoke denitrating process. The device pre-heats constant temperature smoke by means of denitrated smoke, so that smoke residual heat is better utilized. The ammonia spraying mechanism is arranged in front of the heat exchanger to form a turbulent flow element by a fined tube, so that the mixing uniformity of smoke and ammonia is effectively improved, the denitrating efficiency is improved, ammonia escape is prevented, and no ammonia mixing gratings are arranged, so that the structure of the device is simplified and the equipment investment is saved.
Description
Technical field
The utility model relates to the denitrating flue gas treating apparatus, particularly relates to stingy amount normal temperature denitrating flue gas treating apparatus.
Background technology
The whole world enters the NO of atmosphere every year
xTotal amount approximately reaches 5,000 ten thousand tons, and 2008, China NO
xDischarge capacity has reached 2,000 ten thousand tons, becomes the large discharging of the first in the world state.Do not control if do not take measures, expect the year two thousand twenty, NO
xDischarge capacity will reach 3,000 ten thousand tons, and China the Eleventh Five-Year Plan period cuts down the effort of sulfur dioxide 10%, also will be because of NO
xThe remarkable rising of discharge capacity and all offsetting.At present, China is with NO
xInclude overall control category during " 12 " in as the binding indicator.Be discharged into the NO in atmosphere
xMainly contain three sources: power plant's (accounting for 46%), vehicle exhaust (accounting for 49%) and oil-refining chemical factory (accounting for 5%).
In FCC technique, catalyst granules is repeatedly cycling between catalytic cracking reaction zone and catalyst regeneration zones, and at regeneration period, the coke from cracking reaction on catalyst granules is at high temperature removed by air oxidation, make the activity recovery of catalyst, and again utilize in cracking reaction.NO in the FCC flue gas
xMain burning from nitrogenous coke on catalyst, so all can there be NO in the FCC apparatus of all processing nitrogen-containing materials
xEmission problem.NO in the FCC flue gas
xAmount generally accounts for the full NO of factory
x50% of discharge capacity is the NO of oil plant maximum
xEmission source.In the FCC raw material, nitrogen content generally 0.05%～0.35%, approximately 45% enters fluid product in raw material nitrogen, approximately 10% enters gas products, and all the other enter in coke.Nitrogen in coke approximately has 10%～30% to enter flue gas as NO, and all the other are reduced to N by coke and CO
2Discharging.
Gas denitrifying technology mainly contains at present: the SCR method (selective catalytic reduction) of gas-phase reaction and SNCR method (SNCR method), liquid absorption method, solid absorption method, high energy electron active oxidation method etc.
The SCR method is under catalyst action, utilize reducing agent selectively with flue gas in NOx reaction, and generate the N of nonhazardous effect
2And H
2The technology of O, its reducing agent can be ammonia, ammoniacal liquor or urea, also can select CO or H
2, also can select little molecule alkane.The SCR technology is compared with other technologies, has a denitration efficiency high, and thermal discharge is little, and the advantages such as technology maturation are to use maximum technology in Flue Gas Denitrification Engineering both at home and abroad at present.
The SNCR method is under the effect that there is no catalyst, sprays into reducing agent (generally using ammonia, ammoniacal liquor or urea) in the burner hearth of 900 ~ 1100 ℃, and the rapid pyrolysis of reducing agent is NH
3, with the NOx reaction generation nitrogen (N in flue gas
2) and water (H
2O), have certain oxygen to exist in burner hearth, the reducing agent that sprays into optionally with NOx, substantially not with oxygen reaction.If FCC apparatus has been equipped with the CO boiler, SNCR can directly use.The upstream that ammonia is expelled to the CO boiler makes NH
3React in the CO boiler with NOx.NOx in this method removes scope and is limited in 40-60%.It is worth noting, can cause ammonium sulfate to be deposited in the CO boiler by height if the SOx in FCC tail gas contains.NSCR refers to that NOx in source of the gas under uniform temperature and catalyst action, is reduced agent and is reduced to N2, simultaneously reducing agent also with source of the gas in O
2Reaction generates H
2O and CO
2, in this denitrification process, reaction needs the catalytic action by means of catalyst, and reducing agent and NOx and O
2All react, non-selectivity is therefore be called non-selective catalytic reduction.
CN201524525U has introduced a kind of SCR equipment for denitrifying flue gas, it comprises that catalytic reactor, ammonia/air mixer, ammonia spray barrier, air preheater, wherein an end of catalytic reactor connects by economizer and boiler tube, the other end connects by air preheater and dedusting organ pipe, one entrance and the dilution air pipe of described ammonia/air mixer connect, and another entry sequence pipe of described ammonia/air mixer is connected to ammonia dashpot, ammonia evaporator, liquefied ammonia storage tank.The weak point of this structure is, the inside reactor smoke distribution is inhomogeneous, affects denitration efficiency, and produces the escaping of ammonia; Simultaneously, catalytic reactor is placed in the boiler outside, and floor space is large, and equipment investment is high.
CN201454505U has introduced a kind of SCR Benitration reactor, fully mixes with ammonia at the gas approach place through the flue gas after dedusting, desulfurization, then enters in the Benitration reactor shell via reactor inlet, and mist passes through beds, NO
XWith NH
3React under catalyst action, reach the purpose of denitration.The weak point of this structure is, flue gas just directly enters reactor without buffering, causes in reactor smoke distribution inhomogeneous, affect denitration efficiency, and the generation the escaping of ammonia.
The utility model content
Not enough for prior art, the utility model provides a kind of denitrification apparatus for stingy amount normal temperature denitrating flue gas, the denitration efficiency that is intended to solve the interior inhomogeneous generation of smoke distribution of Benitration reactor in prior art descends and the escaping of ammonia, and the plant area area is large, the problem that equipment investment is high.
Stingy amount normal temperature equipment for denitrifying flue gas of the present utility model comprise from top to bottom air inlet section, spray ammonia element, heat exchanger, electric heater, Benitration reactor be connected with the connection flue Wherein, described Benitration reactor comprises several beds, and each beds comprises hanging beam, steam sootblower, catalyst module and catalyst brace summer; It is characterized in that, described heat exchanger comprises condensation chamber and vaporization chamber, and condensation chamber is arranged between spray ammonia element and electric heater, and vaporization chamber is set up in parallel the outside in condensation chamber, and is connected with the Benitration reactor outlet by connecting flue.Heat exchanger is heat exchange of heat pipe, can adopt structure well known to those skilled in the art.
According to equipment for denitrifying flue gas of the present utility model, wherein said heat exchanger is heat exchange of heat pipe, and heat exchanger tube runs through denitrification apparatus and is obliquely installed, and its condensation end is positioned at condensation chamber, and evaporation ends is positioned at vaporization chamber, and condensation end is higher than evaporation ends.
In equipment for denitrifying flue gas of the present utility model, described heat exchange of heat pipe and electric heater all adopt the fin heat exchange pipe structure.
In equipment for denitrifying flue gas of the present utility model, described spray ammonia element can adopt the conventional ammonia-spraying grid in this area.In order further to increase the mixed effect of flue gas and ammonia, avoid the generation of the escaping of ammonia.The spray ammonia element of the following structure of recommendation in the utility model.Described spray ammonia element mainly comprises nozzle, anemostat and spatters plate, and wherein, anemostat comprises expansion segment, trunnion and contraction section three parts, spatters plate and is at least two-layerly, spatters plate and is provided with perforate.Nozzle-axis and anemostat dead in line, and extend in the anemostat contraction section, the angle of throat scope of contraction section is 10 ° ~ 60 °; Nozzle makes each anemostat suction flue gas area coincidence along the intensive layout in flue cross section, guarantees the even distribution of ammonia; Length of throat is 1 ~ 3 times of throat pipe diameter; Mixed flue gas slows down in expansion segment, and fully mixes, and the angle of flare scope of expansion segment is 7 ° ~ 30 °; Spatter plate axis and anemostat dead in line, spatter plate and expansion segment the outlet horizontal cross-section distance be generally 30%～150% of length of throat, preferred 80%～120%.Multilayer is spattered ground floor in plate and is spattered board diameter greater than anemostat lower end outlet diameter, and all the other spatter board diameter and dwindle gradually, spatter plate percent opening 10% ~ 60%.In the utility model, before described spray ammonia element is arranged on heat exchanger, the fin heat exchange pipe that can take full advantage of in heat exchanger and heater forms turbulent element, strengthen ammonia and flue gas mixed effect, improve denitration efficiency and prevent the escaping of ammonia, and need not to arrange mixed ammonia grid, simplified device structure, save equipment investment.
In the utility model, in the spray ammonia element of recommendation, the described plate that spatters also can be the individual layer blind plate structure.Spatter the plate shape and can be circular, square, rectangle or polygon, preferable shape is consistent with outlet, anemostat lower end shape.Described nozzle, anemostat and the dead in line of spattering plate are spattered the plate sectional area greater than the lower end discharge area of expansion segment, spatter plate and expansion segment the outlet horizontal cross-section distance be generally 30%～150% of length of throat, preferred 80%～120%.
Because the SCR reaction needed is carried out 350 ℃ of left and right, when processing stingy amount normal temperature flue gas, need flue gas is heated, simultaneously, do not emit heat owing to neither absorbing heat in the SCR course of reaction yet, therefore, utilize denitration in the utility model denitrification apparatus after flue gas the normal temperature flue gas is carried out preheating, heat is fully used, energy savings; For stingy amount flue gas, adopt Electric heating, neither can significantly increase energy consumption, can guarantee shorter heat time heating time again; By being arranged on the efficient spray ammonia element before Benitration reactor, guarantee the even distribution of ammonia in whole reactor cross section scope, give full play to catalyst performance, guarantee denitration efficiency and prevent the escaping of ammonia; By spray ammonia element was set before heat exchanger, can utilize the fin heat exchange pipe in heat exchanger and heater to form turbulent element, strengthen ammonia and flue gas mixed effect, improve denitration efficiency and prevent the escaping of ammonia, and need not to arrange mixed ammonia grid, simplified device structure, save equipment investment.
Compared with prior art, the CO boiler with denitration function described in the utility model has following advantage:
1, equipment for denitrifying flue gas described in the utility model adopts electrical heating to process stingy amount normal temperature flue gas, significantly not increasing under the prerequisite of energy consumption, can guarantee shorter heat time heating time, but increases the smoke treatment type, improves the denitrating technique scope of application; Due to neither also not heat release of heat absorption of SCR reaction, by flue gas after utilizing denitration, the normal temperature flue gas is carried out preheating, better utilize fume afterheat, reduce the power demand to electric heater, heat is fully used, energy savings.
2, equipment for denitrifying flue gas described in the utility model, to spray before the ammonia mixed organization is arranged on heat exchanger, utilize on the one hand the finned tube on the evaporator section heat exchanger to form turbulent element, can effectively improve flue gas and ammonia mixture homogeneity, improve denitration efficiency and prevent the escaping of ammonia, and need not to arrange mixed ammonia grid, simplified device structure, save equipment investment.
3, CO boiler with denitration function described in the utility model, adopt efficient spray ammonia mixed organization, the wherein said plate that spatters is three layers, ground floor spatters the plate sectional area greater than expansion segment lower end discharge area, make mist form the solid-cone range of distribution after spattering plate, and produce larger dispersion territory, what increase mist and the flue gas that is not inhaled into anemostat mixes probability again, flue gas is mixed more abundant with ammonia, guarantee that in whole reactor cross section scope, ammonia evenly distributes, give full play to catalyst performance, improve denitration efficiency and prevent the escaping of ammonia, reduce and mix needed space, reduce investment outlay.
4, CO boiler with denitration function described in the utility model, adopt efficient spray ammonia mixed organization, the wherein said plate that spatters is the individual layer blind plate, spatter the plate sectional area greater than expansion segment lower end discharge area, the gas of ejection forms in the whirlpool at the place of keeping to the side below spattering plate, what increase mist and the flue gas that is not inhaled into anemostat mixes probability again, produce larger dispersion territory, flue gas is mixed more abundant with ammonia, guarantee that in whole reactor cross section scope, ammonia evenly distributes, give full play to catalyst performance, improve denitration efficiency and prevent the escaping of ammonia, reduce and mix needed space, reduce investment outlay.
Description of drawings
Fig. 1 is the structural representation of the stingy amount normal temperature of the utility model equipment for denitrifying flue gas.
Fig. 2 is a kind of structural representation that sprays the ammonia mixed organization that uses in the utility model device.
Fig. 3 is the structure chart of the described spray ammonia of Fig. 2 element.
Fig. 4 is the structural representation of the another kind spray ammonia mixed organization of use in installing in the utility model.
Fig. 5 is the structure chart of the described spray ammonia of Fig. 4 element.
The specific embodiment
Further illustrate concrete scheme and the occupation mode of the utility model denitrification apparatus below in conjunction with accompanying drawing.
As shown in Figure 1, stingy amount normal temperature equipment for denitrifying flue gas of the present utility model comprises air inlet section 1, spray ammonia mixed organization 2 from top to bottom, heat exchanger 3, electric heater 4, Benitration reactor 5 be connected flue 6.Wherein, Benitration reactor 5 comprises several beds.Each beds forms by hanging beam 7, steam sootblower 8, catalyst module 9 and catalyst brace summer 10.Heat exchanger 3 is comprised of condensation chamber 11 and vaporization chamber 12, and condensation chamber 11 is between spray ammonia mixed organization 2 and electric heater 4, and vaporization chamber 12 is set up in parallel with condensation chamber 11, is positioned at outside denitrification apparatus.Vaporization chamber 12 is connected with the exhanst gas outlet of Benitration reactor 5 by connecting flue 6; Before electric heater 4 is positioned at Benitration reactor 5.
In conjunction with shown in Figure 1, the utility model denitrification apparatus in use, the hanging beam 7 by Benitration reactor 5 interior settings hangs in Benitration reactor 5 with catalyst module 9, and is placed on catalyst brace summer 10, completes the installation of catalyst module; Flue gas enters Benitration reactor 5 through air inlet section 1, at first fully mix with ammonia by spray ammonia mixed organization 2, guarantee the even distribution of ammonia in whole reactor cross section scope, mixed flue gas carries out preheating through the condensation chamber 11 of heat exchanger 3, further be heated to 350 ℃ of left and right in electric heater 4 through the flue gas after preheating, and utilize the fin heat exchange pipe in heat exchanger and heater to form turbulent element, strengthen ammonia and flue gas mixed effect; Then enter Benitration reactor 5, and carry out reduction reaction and remove NO on catalyst module 9
XFlue gas after processing enters the vaporization chamber 12 of heat exchanger 3 through connecting flue 6, the evaporation ends of heat exchanger heats, and the normal temperature flue gas is carried out preheating, Mist heat recovering.After completing heat recovering process, but flue gas discharging directly into atmosphere or enter desulfurizer.Dust content increases in flue gas, during the blocking catalyst duct, needs to start steam sootblower 8 and blow ash.
According to equipment for denitrifying flue gas of the present utility model, wherein said spray ammonia mixed organization can adopt conventional ammonia-spraying grid.In the utility model, recommendation has the spray ammonia mixed organization of following structure.Fig. 2 to Fig. 4 has provided the structural representation of the spray ammonia mixed organization of two kinds of different structures.
As shown in Figure 2, in boiler described in the utility model, described spray ammonia mixed organization 2 comprises spray ammonia house steward 21, spray ammonia arm 22 and spray ammonia element 23, and described spray ammonia arm 22 arranges some, one end of spray ammonia arm 22 is connected with spray ammonia house steward 21, and the other end is enclosed construction; Described spray ammonia element 23 comprises nozzle 24, anemostat 25 and spatter plate 26, and the lower surface of spray ammonia arm 22 is connected with described spray ammonia element 23 by nozzle 24.Described anemostat 25 comprises contraction section 27, trunnion 28 and expansion segment 29 from top to bottom successively, and nozzle 24 lower ends outlets are stretched in anemostat contraction section 25, describedly spatters the below that plate 26 is arranged at expansion segment 29.Wherein, the contraction section angle of throat is 15 °～30 °, 10 °～20 ° of the expansion segment angles of flare, length of throat is 1～3 times of throat pipe diameter, spatter plate and expansion segment the outlet horizontal cross-section distance be 80%～120% of length of throat.The described plate 26 that spatters is three layers, and plate is provided with sieve aperture, ground floor spatters the plate sectional area greater than the lower end discharge area of expansion segment 29, all the other two-layer plate sectional areas that spatter dwindle gradually, the described plate percent opening that spatters is 30%～50%, the aperture of spattering sieve aperture on plate generally can be 4～6mm, adopts equilateral triangle to arrange or square is arranged, and the adjacent sieve aperture that spatters between plate is staggered.
In conjunction with Fig. 3, the operation principle of spray ammonia mixed organization shown in Figure 2 is: ammonia enters spray ammonia arm 22 through spray ammonia house steward 21, spray into anemostat contraction section 27 by the nozzle 24 on spray ammonia arm 22, and in the interior acceleration of contraction section 27, form negative pressuren zone, produce swabbing action and suck near the most of flue gas of contraction section 27 entrances, mist passes trunnion 28 and enters anemostat expansion segment 29, and slow down in expansion segment 29, realize that the phase I of two kinds of gases mixes; Mist is spattering plate 26 places generation splash, utilization is spattered 26 pairs of simulation model for mixing gases flows of plate and is formed obstruction, make mist form the solid-cone range of distribution after spattering plate 26, what increase mist and the flue gas that is not inhaled into anemostat 23 mixes probability again, and produce larger dispersion territory, realize that mist mixes with the second stage that is not inhaled into anemostat 23 flue gases, thereby reach good mixed effect.
Fig. 4 has provided the spray ammonia mixed organization of another kind of structure.As shown in Figure 4, described spray ammonia mixed organization 2 comprises spray ammonia house steward 21, spray ammonia arm 22 and spray ammonia element 23, and described spray ammonia arm 22 arranges some, and an end of spray ammonia arm 22 is connected with spray ammonia house steward 21, and the other end is enclosed construction; Described spray ammonia element 23 comprises nozzle 24, anemostat 25 and spatter plate 26, and the lower surface of spray ammonia arm 22 is connected with described spray ammonia element 23 by nozzle 24.Described anemostat 25 comprises contraction section 27, trunnion 28 and expansion segment 29 from top to bottom successively, and nozzle 24 lower ends outlets are stretched in anemostat contraction section 25, describedly spatters the below that plate 26 is arranged at expansion segment 29.Wherein, the contraction section angle of throat is 15 °～30 °, 10 °～20 ° of the expansion segment angles of flare, length of throat is 1～3 times of throat pipe diameter, spatter plate and expansion segment the outlet horizontal cross-section distance be 80%～120% of length of throat; The described plate 26 that spatters is the individual layer blind plate, spatters the plate sectional area greater than the lower end discharge area of expansion segment 29.
In conjunction with Fig. 5, the operation principle of spray ammonia mixed organization shown in Figure 4 is: ammonia enters spray ammonia arm 22 through spray ammonia house steward 21, spray into anemostat contraction section 27 by the nozzle 24 on spray ammonia arm 22, and in the interior acceleration of contraction section 27, form negative pressuren zone, produce swabbing action and suck near the most of flue gas of contraction section 27 entrances, mist passes trunnion 28 and enters anemostat expansion segment 29, and slow down in expansion segment 29, realize that the phase I of two kinds of gases mixes; Mist is spattering plate 26 places generation splash, the place form to stay the whirlpool, and what increase mist and the flue gas that is not inhaled into anemostat 23 mixes probability again, and generation larger dispersion territory, realize that mist mixes with the second stage that is not inhaled into anemostat 23 flue gases, reaches good mixed effect.
Claims (11)
1. a stingy amount normal temperature equipment for denitrifying flue gas, is characterized in that, described device comprise from top to bottom air inlet section, spray ammonia element, heat exchanger, electric heater, Benitration reactor be connected with the connection flue Wherein said Benitration reactor comprises several beds, and each beds comprises hanging beam, steam sootblower, catalyst module and catalyst brace summer; Described heat exchanger comprises condensation chamber and vaporization chamber, and condensation chamber is arranged between spray ammonia element and electric heater, and vaporization chamber is set up in parallel the outside in condensation chamber, and is connected with the Benitration reactor outlet by connecting flue.
2. according to device claimed in claim 1, it is characterized in that, described heat exchanger is heat exchange of heat pipe, and heat exchanger tube is obliquely installed, and its condensation end is positioned at condensation chamber, and evaporation ends is positioned at vaporization chamber, and condensation end is higher than evaporation ends.
3. according to device claimed in claim 1, it is characterized in that, described heat exchange of heat pipe and electric heater all adopt the fin heat exchange pipe structure.
4. according to device claimed in claim 1, it is characterized in that, described spray ammonia element adopts ammonia-spraying grid.
5. according to device claimed in claim 1, it is characterized in that, described spray ammonia element comprises nozzle, anemostat and spatters plate, and described anemostat comprises expansion segment, trunnion and contraction section three parts, and the described plate that spatters is at least two-layerly, spatters plate and is provided with perforate.
6. according to device claimed in claim 5, it is characterized in that, described nozzle-axis and anemostat dead in line, and extend in the anemostat contraction section.
7. according to device claimed in claim 5, it is characterized in that, the angle of throat of described contraction section is 10 ° ~ 60 °, length of throat is 1 ~ 3 times of throat pipe diameter, the angle of flare of expansion segment is 7 ° ~ 30 °, spatter plate axis and anemostat dead in line, spatter plate and expansion segment the outlet horizontal cross-section distance be generally 30%～150% of length of throat.
8. according to device claimed in claim 5, it is characterized in that, the described ground floor that spatters in plate spatters board diameter greater than anemostat lower end outlet diameter, and all the other spatter board diameter and dwindle gradually.
9. according to device claimed in claim 1, it is characterized in that, described spray ammonia element comprises nozzle, anemostat and spatters plate, and described anemostat comprises expansion segment, trunnion and contraction section three parts, and the described plate that spatters is the individual layer blind plate structure.
10. according to device claimed in claim 8, it is characterized in that, described spatter plate be shaped as circle or polygon, described nozzle, anemostat and the dead in line of spattering plate, spatter the plate sectional area greater than the lower end discharge area of expansion segment, spatter plate and expansion segment the outlet horizontal cross-section distance be 30%～150% of length of throat.
11. according to device claimed in claim 1, it is characterized in that, it is consistent that described that spatter plate and anemostat lower end go out mouth-shaped.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220546214 CN202962277U (en) | 2012-10-24 | 2012-10-24 | Small air quantity constant temperature smoke denitrating device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220546214 CN202962277U (en) | 2012-10-24 | 2012-10-24 | Small air quantity constant temperature smoke denitrating device |
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|---|---|
| CN202962277U true CN202962277U (en) | 2013-06-05 |
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|---|---|---|---|
| CN 201220546214 Expired - Lifetime CN202962277U (en) | 2012-10-24 | 2012-10-24 | Small air quantity constant temperature smoke denitrating device |
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| CN105091008A (en) * | 2015-09-10 | 2015-11-25 | 东南大学 | Temperature-controllable selective catalytic reduction (SCR) denitration reaction catalytic device of thermal power plant |
| CN106422711A (en) * | 2016-11-17 | 2017-02-22 | 上海华之邦科技股份有限公司 | High-efficiency denitrification equipment |
| CN106422710A (en) * | 2016-11-17 | 2017-02-22 | 上海华之邦科技股份有限公司 | High-capacity denitration apparatus |
| CN106474753A (en) * | 2016-03-24 | 2017-03-08 | 梅丽中 | A kind of bittern crystallizing and drying device |
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2012
- 2012-10-24 CN CN 201220546214 patent/CN202962277U/en not_active Expired - Lifetime
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| CN105091008A (en) * | 2015-09-10 | 2015-11-25 | 东南大学 | Temperature-controllable selective catalytic reduction (SCR) denitration reaction catalytic device of thermal power plant |
| CN106474753A (en) * | 2016-03-24 | 2017-03-08 | 梅丽中 | A kind of bittern crystallizing and drying device |
| CN106474753B (en) * | 2016-03-24 | 2019-01-29 | 青岛果子知识产权运营有限公司 | A kind of brine crystallizing and drying device |
| CN106422711A (en) * | 2016-11-17 | 2017-02-22 | 上海华之邦科技股份有限公司 | High-efficiency denitrification equipment |
| CN106422710A (en) * | 2016-11-17 | 2017-02-22 | 上海华之邦科技股份有限公司 | High-capacity denitration apparatus |
| CN107042048A (en) * | 2017-03-16 | 2017-08-15 | 华南理工大学 | A kind of gravity heat-pipe type defogging method and demister |
| CN109482065A (en) * | 2017-09-09 | 2019-03-19 | 中国石油化工股份有限公司 | A kind of denitration process method of ethane cracking furnace discharge flue gas |
| CN109482065B (en) * | 2017-09-09 | 2021-04-06 | 中国石油化工股份有限公司 | Denitration treatment method for exhaust gas of ethylene cracking furnace |
| CN114082299A (en) * | 2021-11-09 | 2022-02-25 | 南京工业大学 | Heat pipe type SCR denitration reactor and method for denitration of low-temperature sulfur-containing flue gas by using same |
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