CN108325385A - It improves low-temperature SCR catalyst activity and inhibits by-product N2The SCR reactors of O - Google Patents
It improves low-temperature SCR catalyst activity and inhibits by-product N2The SCR reactors of O Download PDFInfo
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- CN108325385A CN108325385A CN201810347148.0A CN201810347148A CN108325385A CN 108325385 A CN108325385 A CN 108325385A CN 201810347148 A CN201810347148 A CN 201810347148A CN 108325385 A CN108325385 A CN 108325385A
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- 239000003054 catalyst Substances 0.000 title claims abstract description 136
- 239000006227 byproduct Substances 0.000 title claims abstract description 35
- 230000000694 effects Effects 0.000 title abstract description 34
- 238000009792 diffusion process Methods 0.000 claims abstract description 63
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000003546 flue gas Substances 0.000 claims abstract description 34
- 239000008246 gaseous mixture Substances 0.000 claims abstract description 33
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000007789 gas Substances 0.000 claims abstract description 19
- 239000000779 smoke Substances 0.000 claims abstract description 8
- 230000001413 cellular effect Effects 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 description 24
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 23
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 16
- 239000003638 chemical reducing agent Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 9
- 230000007246 mechanism Effects 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- 238000010531 catalytic reduction reaction Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000004458 analytical method Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000007086 side reaction Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 150000004706 metal oxides Chemical class 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound [N].N CVTZKFWZDBJAHE-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 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000002401 inhibitory effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000000738 capillary electrophoresis-mass spectrometry Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000009533 lab test Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 230000007480 spreading Effects 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/88—Handling or mounting catalysts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/90—Injecting reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The present invention provides a kind of raising low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, include smoke inlet by the flow direction of flue gas, reactor body and exhanst gas outlet, it is internally provided with the catalyst bed for placing low-temperature SCR catalyst in reactor body, ammonia nitrogen gaseous mixture diffuser group is fitted in catalyst bed, ammonia nitrogen gaseous mixture diffuser group includes ammonia nitrogen gaseous mixture input pipe and at least two rows of diffusion manifold arranged side by side from top to bottom, often row's diffusion manifold is made of horizontally disposed more diffusers, more diffusion branch pipes are connected separately on every diffuser, ammonia nitrogen gaseous mixture input pipe is connected between external ammonia nitrogen mixed gas feeder and each diffusion manifold, several diffusion holes are offered on each diffuser and each diffusion branch pipe.The present invention is conducive to improve low temperature catalyst activity, improves low-temperature catalyzed denitration efficiency, while reaching control by-product N2The effect of O is generated.
Description
Technical field
The present invention relates to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O belong to environmental protection
Filed of flue gas purification.
Background technology
A large amount of high-temp combustion process is often referred in metallurgy industry, to produce a large amount of nitrogen oxides (NOx).
Likewise, in Chemical Manufacture, oil gas refining, coal-fired power generation field, the flue gas rich in NOx also will produce.Above-mentioned field discharge
Flue gas is required for by denitration process to meet the requirement of environmental protection.Denitration process refers to that generated NOx is reduced to N2,
To remove the NOx in flue gas, main denitrating technique is divided into the prior art：Selective catalytic reduction technique (english abbreviation
For SCR) and selective non-catalytic reduction technique (english abbreviation SNCR).
Wherein, selective catalytic reduction denitration technology (SCR) is the gas denitrifying technology being most widely used at present, it
There is no by-product, do not form secondary pollution, apparatus structure is simple, and high (up to 90% or more) with removal efficiency, operation
Reliably, convenient for safeguarding the advantages that.
SCR technology principle is：Under the action of catalyst, ammonia is sprayed into the flue gas of certain temperature, by NOXIt is reduced into N2With
H2O.But current SCR catalyst mainly for denitration operating mode be NOx under the conditions of high temperature (220 DEG C~420 DEG C) de-
Go out, and the flue-gas temperature for needing denitration generated in practical metallurgical production process is all relatively low, for example sintering flue gas generally exists
120 DEG C or so, coking flue gas is at 200 DEG C or so.In addition, flue gas it may also be desirable to by just can be into after the techniques such as dust-removal and desulfurizing
Enter in SCR reactors, often more required denitration reaction temperature is lower for flue-gas temperature at this time, needs to use heating equipment pair
Flue gas is re-fed into after being heated in SCR reactors, and heating flue gas certainly will bring energy consumption problem.Therefore, low-temperature denitration catalyst
Use can efficiently control purification abjection cost, now widely used low-temperature SCR catalyst all be use V-Mn systems
The introducing of the catalyst of catalyst or similar formula, Mn base oxides can effectively improve low-temperature SCR catalyst activity, but
It is that laboratory research finds that the addition of Mn base oxides can bring N2Selectivity decline the problem of, though at present the country steel plant or
Be power plant emission end flue gas discharge continuous monitoring system (english abbreviation CEMS) data in only to NO and NO2Concentration of emission is made
For object of supervision, actually Mn base oxides can promote N2The generation of O, so actually containing phase in seeming purified gas up to standard
As the N of content2O, and N2O can not only destroy ozone layer, this kind of gas or one kind being equivalent to equivalent CO2The greenhouse that 300 times of gas
Gas on the destruction of environment and influences very serious.
Invention content
To overcome the defect of above-mentioned technology, according to the feature for using low-temperature SCR catalyst at present, analysis SCR reactions are being urged
Reaction mechanism in agent and path, technical problem to be solved by the invention is to provide one kind to be conducive to improve low temperature catalyst
Activity improves low-temperature catalyzed denitration efficiency, while reaching control by-product N2The SCR reactors that O is generated.
To achieve the above object, a kind of raising low-temperature SCR catalyst of present invention offer is active and inhibits by-product N2O's
SCR reactors include successively smoke inlet, reactor body and exhanst gas outlet, in the reaction by the flow direction of flue gas
Device body interior is equipped with the catalyst bed for placing low-temperature SCR catalyst, and ammonia nitrogen is fitted in the catalyst bed
Gaseous mixture diffuser group, the ammonia nitrogen gaseous mixture diffuser group include ammonia nitrogen gaseous mixture input pipe and are from top to bottom arranged side by side
At least two rows of diffusion manifold, often arrange the diffusion manifold and are made of horizontally disposed more diffusers, on every diffuser respectively
More diffusion branch pipes are connected with, the ammonia nitrogen gaseous mixture input pipe is connected to external ammonia nitrogen mixed gas feeder and each expansion
Between dissipating manifold, several diffusion holes are offered on each diffuser and each diffusion branch pipe.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein described
Catalyst bed is cellular integrated catalyst bed, and the cellular integrated catalyst bed includes longitudinally spaced cloth
If at least two layers of catalyst sub-bed layer, every layer of catalyst sub-bed layer along the cross section of the reactor body by being bolted together
Multiple catalyst bed layer units constitute, each catalyst bed layer unit includes bed framework and intersects in the bed framework
The bed demarcation strip of setting；The diffusion branch pipe is laid in the cross section of the reactor body perpendicular to the diffuser,
The opening direction of the diffusion hole is longitudinally consistent with the reactor body.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein described
Catalyst sub-bed layer is 2 to 4 layers.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein described
It is 0.8m~1.2m, preferably 1m~1.1m to spread the spacing between the adjacent diffuser of manifold.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein described
Catalyst bed be granular pattern catalyst filling bed, the granular pattern catalyst filling bed include monoblock type bed framework and
The bed demarcation strip arranged in a crossed manner in the monoblock type bed framework；The more diffusion branch pipes are respectively in the reactor master
It is laid perpendicular to the diffuser in the cross section and longitudinal section of body, the opening direction of the diffusion hole is filled out towards the granular pattern
Fill the inside circumference of catalyst bed.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein described
It is 1.2m~2m, preferably 1.5m~1.6m to spread the spacing between the adjacent diffuser of manifold.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein each institute
It is 0.6m~1m to state the distance between adjacent described diffuser branch pipe on diffuser, preferably by for 0.7m~0.8m, respectively
The length of the diffuser branch pipe is 0.4m~0.6m.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein described
Percent opening of the diffusion hole on the diffuser and the diffusion branch pipe is 4%~12%, preferably 5%~10%, is more selected as
7%~8%.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein each
The aperture of the diffusion hole is 1mm~5mm, preferably 2mm~3mm.
It is as described above to improve low-temperature SCR catalyst activity and inhibit by-product N2The SCR reactors of O, wherein in institute
It states and is equipped with deflector and flow straightening grid at smoke inlet.
Compared with prior art, the present invention has following advantageous effects：
1, the configuration of the present invention is simple had both facilitated processing without increasing volume and external hanging device, was also conducive to existing dress
It sets and is transformed；
2, ammonia nitrogen gaseous mixture is directly released into catalyst bed by the present invention by diffuser, can be improved in catalyst bed
The NH adsorbed on layer3Amount achievees the purpose that improve catalytic activity；
3, the present invention can be ensured using the design that ammonia nitrogen gaseous mixture is directly discharged into catalyst bed in reaction office
The relative saturation of reducing agent within the scope of portion, prevents due to reducing agent NH3Deficiency cause side reaction generate N2The case where O, occurs, together
When reduce NH3In wet flue gas with SO2The time of contact improves reducing agent service efficiency, enhances denitration effect；
4, the diffusion guard system designed by the present invention can be also adjusted according to actual needs, reach full and uniform release
The effect of nitrogen ammonia gaseous mixture is to catalyst bed.
Description of the drawings
Fig. 1 is that the present invention improves low-temperature SCR catalyst activity and inhibits by-product N2The embodiment of the SCR reactors of O
One structural schematic diagram；
Fig. 2 is the reactor body inside top figure of Fig. 1；
Fig. 3 is the enlarged structure schematic diagram of part A in Fig. 2；
Fig. 4 is that the present invention improves low-temperature SCR catalyst activity and inhibits by-product N2The embodiment of the SCR reactors of O
Two structural schematic diagram.
Figure label has following meaning：
1- smoke inlets；2- reactor bodies；3- exhanst gas outlets；4- deflectors；5- flow straightening grids；6- catalyst beds；
61- monoblock type bed frameworks；62- bed demarcation strips；7- ammonia nitrogen gaseous mixture diffuser groups；71- ammonia nitrogen gaseous mixture input pipes；72-
Spread manifold；73- diffusers；74- spreads branch pipe；75- diffusion holes；9- catalyst sub-bed layers；91- catalyst bed layer units；
The split type bed frameworks of 911-；912- bed demarcation strips.
Specific implementation mode
In order to which technical characteristic, purpose and the advantageous effect to the present invention are more clearly understood, in conjunction with specific implementation
Example and technical scheme of the present invention is carried out described further below, it should be understood that these examples be merely to illustrate the present invention rather than
It limits the scope of the invention.In embodiment, each Starting reagents material is commercially available, test method without specific conditions
For conventional method known to fields and normal condition, or according to the condition proposed by apparatus manufacturer.
In the present invention, low-temperature SCR catalyst is existing catalyst, is using V-Mn series catalysts or similar formula
Catalyst.
In the present invention, SCR refers to selective catalytic reduction (selective catalytic reduction), is utilized
Catalyst and reducing agent are to NOxFlue gas carries out the prior art of reduction purification.
L-H (full name in English：Langmuir-Hinshelwood) mechanism refers to NH3B of the gas molecule in catalyst surface
It adsorbs to form NH in sour position4 +, further with catalyst surface by NO/NO2The cigarette nitrate that reaction is formed, which further reacts, generates N2
And H2The reaction process of O.
E-R (full name in English：Eley-Rideal) mechanism refers to NH3Gas molecule is adsorbed in the L acid position of catalyst surface
And dehydrogenation forms NH2, further reacted with the NO of gas phase and generate N2And H2The reaction process of O.
As shown in Figure 1, improving low-temperature SCR catalyst activity for the present invention and inhibiting by-product N2The SCR reactors of O
One structural schematic diagram of embodiment.The present invention improves low-temperature SCR catalyst activity and inhibits by-product N2The SCR reactors of O, are pressed
The flow direction (referring to arrow direction in Fig. 1) of flue gas, successively include smoke inlet 1, reactor body 2 and exhanst gas outlet 3,
It is equipped with deflector 4 and flow straightening grid 5 successively along the flow direction of flue gas at smoke inlet 1, keeps external flue gas uniform
Into being reacted in reactor body 2.It is internally provided with the catalyst for placing low-temperature SCR catalyst in reactor body 2
Bed 6, is fitted with ammonia nitrogen gaseous mixture diffuser group 7 in catalyst bed 6, and ammonia nitrogen gaseous mixture diffuser group 7 is mixed including ammonia nitrogen
Gas input pipe 71 and at least two rows of diffusion manifold 72 arranged side by side from top to bottom are closed, often row's diffusion manifold 72 is set by horizontal Tile
The more diffusers 73 set are constituted, and more diffusion branch pipes 74 are connected separately on every diffuser 73 so that each row's diffusion manifold
72 diffuser 73 and diffusion 74 dense distribution of branch pipe is in catalyst bed 6；Ammonia nitrogen gaseous mixture input pipe 71 is connected to outside
Between ammonia nitrogen gaseous mixture feeder (not shown) and each diffusion manifold 72 so that each diffusion manifold 72 is mixed by ammonia nitrogen
It is connected with external ammonia nitrogen mixed gas feeder after 8 parallel connection of gas input pipe, on each diffuser 73 and each diffusion branch pipe 74
Offer several diffusion holes 75 so that (general ammonia level is not higher than 5% to ammonia nitrogen gaseous mixture, and ammonia level can be measured as needed
It is adjusted) it is diffused to inside the catalyst bed 6 in reactor body 2 by diffusion hole 75.With existing SCR reactors phase
Than the contact position of ammonia nitrogen gaseous mixture and flue gas is provided in the catalyst bed 6 for placing low-temperature SCR catalyst by the present invention
Place can play the NH improved in ammonia nitrogen gaseous mixture in this way3It activates with low-temperature SCR catalyst Contact-sorption, is reacted for low-temperature SCR
The effect to create good conditions improves low-temperature SCR catalyst activity；The structure design of the present invention avoids in flue gas simultaneously
NO2Due to NH when part is excessive3Side reaction not enough occurs, plays and inhibits by-product N2The effect of O；Furthermore structure of the invention
Design can reduce SO in former flue gas2With NH3Time of contact, reduce the generation of ammonium sulfate, improve the service efficiency of reducing agent,
SCR catalyst activity can be improved to a certain extent.
As shown in Figure 1 and Figure 2, in embodiment one, catalyst bed 6 is cellular integrated catalyst bed, cellular
Integral catalyst bed layer includes at least two layers of catalyst sub-bed layer 9 of longitudinally spaced laying, it is preferred that catalyst sub-bed layer
9 be 2 to 4 layers, correspondingly, diffusion manifold 72 is equipped with 2 to 4 rows, each row's diffusion manifold 72 is inserted in corresponding each catalyst respectively
In sub-bed layer 9 so that when flue gas sequence is by each catalyst sub-bed layer 9, can be expanded respectively by diffusion hole 75 with diffusion manifold 72
The NH to shed3Haptoreaction.Every layer of catalyst sub-bed layer 9 multiple is urged by what is be bolted together along the cross section of reactor body 2
Agent bed unit 91 is constituted, and each catalyst bed layer unit 91 is including split type bed framework 911 and in split type bed frame
Bed demarcation strip 912 arranged in a crossed manner in body 911,912 groups of bed demarcation strip in adjacent two catalyst bed layer units 91
It is combined to form similar cellular polygonized structure.Multiple diffusion branch pipes 74 are respectively arranged at corresponding diffuser 73
On, and spread branch pipe 74 and lay (as shown in Figure 2) perpendicular to diffuser 73 in the cross section of reactor body 2 so that diffusion
The opening direction in hole 75 is consistent with 2 longitudinal direction of reactor body, the catalyst laid on cellular integrated catalyst bed
It should closely arrange the upper and lower side for being placed in each diffuser 73 being placed in parallel, can to greatest extent make in ammonia nitrogen gaseous mixture
NH3It is activated with low-temperature SCR catalyst Contact-sorption.
In embodiment one, further, spread manifold 72 in adjacent diffuser 73 between spacing be 0.8m~
1.2m, its spacing are preferably 1m~1.1m.The spacing can ensure the NH diffused out by diffuser 733It is come into full contact with instead with flue gas
It answers.
To be further ensured that NH3Come into full contact with and react with flue gas, the adjacent diffuser branch pipe 74 on each diffuser 73 it
Between distance be 0.6m~1m, preferably by for 0.7m~0.8m, the length of each diffuser branch pipe 74 is 0.4m~0.6m；Diffusion
Percent opening of the hole 75 on diffuser 73 and diffusion branch pipe 74 is 4%~12%, preferably 5%~10%, more it is selected as 7%~
8%；The aperture of each diffusion hole 75 is 1mm~5mm, preferably 2mm~3mm.Wherein, percent opening refers to opening for all diffusion holes 75
The hole gross area accounts for the percentage of 73 surface area of all diffusers or all diffusion 74 surface areas of branch pipe.
As shown in figure 4, improving low-temperature SCR catalyst activity for the present invention and inhibiting by-product N2The SCR reactors of O
The structural schematic diagram of embodiment two.The present embodiment two and the structure and principle of embodiment one are essentially identical, and difference essentially consists in,
Catalyst bed 6 uses granular pattern catalyst filling bed, which includes monoblock type bed framework
61 and bed demarcation strip 62 arranged in a crossed manner in the monoblock type bed framework 61, diffusion manifold 72 are whole to be inserted into monoblock type bed
In layer framework 61, low-temperature SCR catalyst is stacked in granular pattern catalyst filling bed and forms irregular air passage.More
Branch pipe 74 is spread to lay perpendicular to corresponding diffuser 73 in the cross section and longitudinal section of reactor body 2 respectively, and
Stereoscopic three-dimensional distributed architecture is formed, diffuser 73 and the opening direction for spreading the diffusion hole 75 on branch pipe 74 are filled towards granular pattern
The inside circumference of catalyst bed is distributed so that NH3It can come into full contact with and react with the flue gas of process from all directions.
In embodiment two, it is 1.2m~2m to spread the spacing between the adjacent diffuser 73 of manifold 72, preferably
1.5m~1.6m, further to ensure NH3It comes into full contact with and reacts with flue gas.
The operation principle of the present invention is that：
For the SCR reactions under low-temperature condition, response path and mechanism had at present a large amount of experimental analysis and
Data result also or the two and is deposited although SCR reactions are L-H mechanism E-R mechanism when educational circles is for low temperature, remains and strive
View, but do not deny that SCR reacts main and NH under low temperature3Adsorption activation on a catalyst is directly related, whether in B acid
Position forms NH4 +Or form NH in the dehydrogenation of L acid position2Species, all to further reaction generates N below2It directly affects, simultaneously
Quick SCR reactions：NO+NO2+2NH3=2N2+3H2Can O occur the reactivity for being also directly related to low-temperature SCR catalyst,
And should be L-H mechanism according to the response path of quick SCR occurs to the analysis of reaction mechanism, it is more that this needs catalyst to have
B acid position, while ensure have enough NO that can be oxidized to NO2, used low-temperature SCR catalyst is all to have so at present
Primary condition, by the addition especially Mn elements of multi-component metal oxide, also compounding aid metal oxide and
Oxide carrier so that this kind of catalyst had both included abundant B acid position, also contained a large amount of L acid position, therefore whether L-H is also
It is the paths E-R, catalyst all has primary condition, it would be appreciated that in laboratory test, it, can be big under cryogenic conditions
Amount generates by-product N2O, this is because NO is oxidized to NO2Excessive velocities after, extra NO2Cannot to participate in quick SCR in time anti-
It answers, at this time NO2Itself SCR reactions can then occur, total equation is：2NO2+4NH3+O2=3N2+6H2O, real reaction process
Very complicated, and this reaction result only occur in reducing agent it is excessive under the conditions of, but discharged according to standard SCR reaction
NH3Generally all it is slightly less than 1 with the ratio of NOx, in this case, intermediate product NH4NO3Release N can then be decomposed2O, here it is
The reason of by-product occurs, when temperature is higher, NH4NO3It can also decompose and generate NO and NO2, conversion rate of NOx is caused to decline；Pass through
Above analysis.The principle of the present invention is exactly to pass through NH3It is provided in placement low-temperature SCR catalyst with the contact position of catalyst
Catalyst bed at, can play in this way improve ammonia nitrogen gaseous mixture in NH3It is activated with low-temperature SCR catalyst Contact-sorption,
It creates good conditions for low-temperature SCR reaction, while avoiding NO2Due to NH when part is excessive3Side reaction not enough occurs, grasps in this way
Make it is also an advantage that being exactly to reduce SO in former flue gas2With NH3Time of contact, reduce the generation of ammonium sulfate, improve reducing agent
Service efficiency can also improve SCR activity to a certain extent.
When in use, reaction is being injected by ammonia nitrogen gaseous mixture input pipe 71 by nitrogen dilution mixed ammonia nitrogen gaseous mixture
In device main body 2, ammonia nitrogen gaseous mixture passes through diffuser 73, is further separated into diffusion branch pipe 74, then by diffuser 73 and diffusion branch pipe 74
On diffusion hole 75 uniformly discharge into catalyst bed 6.
The present invention uses operating temperature for 200 DEG C~220 DEG C of V-Mn-TiO2Low-temperature SCR catalyst, in embodiment one
It is 3 layers, layer height 1.25m that catalyst bed, which uses honeycomb monolith, the catalyst bed number of plies, and ammonia nitrogen gaseous mixture is distributed diffuser
It is arranged in every layer of catalyst bed, every pipe horizontal interval is 1m, and 4 every layer, diffusion branch length of tube is 0.45m, level side
To setting, it is divided into 0.7m between setting, diffusion hole is all uniformly provided on supervisor and branch pipe, aperture 3mm, percent opening 6% will be warm
Degree is introduced into through deflector 4 and flow straightening grid 5 in reaction zone for 190~210 DEG C of coke oven flue gas by Reactor inlet, in flue gas
NOx is 300~800mg/Nm3, SO2For 50~200mg/Nm3, the NO/NO in flue gas2With reducing agent NH3On catalyst bed
SCR reactions occur, are discharged by mouth under reactor after catalyst bed, NOx content is less than 150mg/Nm in flue gas at this time3；
The conversion ratio of NOx is more than 80%.
Technical solution of the present invention has technique effect beneficial below：
1, the configuration of the present invention is simple had both facilitated processing without increasing volume and external hanging device, was also conducive to existing dress
It sets and is transformed；
2, ammonia nitrogen gaseous mixture is directly released into catalyst bed by the present invention by diffuser, can be improved in catalyst bed
The NH adsorbed on layer3Amount achievees the purpose that improve catalytic activity；
3, the present invention can be ensured using the design that ammonia nitrogen gaseous mixture is directly discharged into catalyst bed in reaction office
The relative saturation of reducing agent within the scope of portion, prevents due to reducing agent NH3Deficiency cause side reaction generate N2The case where O, occurs, together
When reduce NH3In wet flue gas with SO2The time of contact improves reducing agent service efficiency, enhances denitration effect；
4, the diffusion guard system designed by the present invention can be also adjusted according to actual needs, reach full and uniform release
The effect of nitrogen ammonia gaseous mixture is to catalyst bed.
What is finally illustrated is：Above example is merely to illustrate the implementation process and feature of the present invention, and unrestricted is sent out
Bright technical solution, although the present invention has been described in detail with reference to the above embodiments, those skilled in the art answer
Work as understanding：It is still possible to modify or equivalently replace the present invention, without departing from the spirit and scope of the present invention any
Modification or part are replaced, and should all be covered in protection scope of the present invention.
Claims (10)
1. a kind of raising low-temperature SCR catalyst is active and inhibits by-product N2The SCR reactors of O, by the flow direction of flue gas,
It includes smoke inlet, reactor body and exhanst gas outlet successively, which is characterized in that is internally provided with use in the reactor body
In the catalyst bed for placing low-temperature SCR catalyst, ammonia nitrogen gaseous mixture diffuser group, institute are fitted in the catalyst bed
It includes that ammonia nitrogen gaseous mixture input pipe and at least two rows arranged side by side from top to bottom spread manifold to state ammonia nitrogen gaseous mixture diffuser group,
It often arranges the diffusion manifold to be made of horizontally disposed more diffusers, more diffusion branch is connected separately on every diffuser
Pipe, the ammonia nitrogen gaseous mixture input pipe is connected between external ammonia nitrogen mixed gas feeder and each diffusion manifold, each
Several diffusion holes are offered on the diffuser and each diffusion branch pipe.
2. raising low-temperature SCR catalyst according to claim 1 is active and inhibits by-product N2The SCR reactors of O,
It is characterized in that, the catalyst bed is cellular integrated catalyst bed, the cellular integrated catalyst bed packet
At least two layers of catalyst sub-bed layer of longitudinally spaced laying is included, every layer of catalyst sub-bed layer is by the cross along the reactor body
Multiple catalyst bed layer units that section is bolted together are constituted, and each catalyst bed layer unit includes bed framework and described
Bed demarcation strip arranged in a crossed manner in bed framework；The diffusion branch pipe is in the cross section of the reactor body perpendicular to institute
Diffuser laying is stated, the opening direction of the diffusion hole is longitudinally consistent with the reactor body.
3. raising low-temperature SCR catalyst according to claim 2 is active and inhibits by-product N2The SCR reactors of O,
It is characterized in that, the catalyst sub-bed layer is 2 to 4 layers.
4. raising low-temperature SCR catalyst according to claim 3 is active and inhibits by-product N2The SCR reactors of O,
It is characterized in that, the spacing between the adjacent diffuser of the diffusion manifold is 0.8m~1.2m, preferably 1m~1.1m.
5. raising low-temperature SCR catalyst according to claim 1 is active and inhibits by-product N2The SCR reactors of O,
It is characterized in that, the catalyst bed is granular pattern catalyst filling bed, and the granular pattern catalyst filling bed includes whole
Body formula bed framework and bed demarcation strip arranged in a crossed manner in the monoblock type bed framework；The more diffusion branch pipe difference
It is laid perpendicular to the diffuser in the cross section and longitudinal section of the reactor body, the opening direction court of the diffusion hole
To the inside circumference of the granular pattern catalyst filling bed.
6. raising low-temperature SCR catalyst according to claim 5 is active and inhibits by-product N2The SCR reactors of O,
It is characterized in that, the spacing between the adjacent diffuser of the diffusion manifold is 1.2m~2m, preferably 1.5m~1.6m.
7. raising low-temperature SCR catalyst according to any one of claim 1 to 6 is active and inhibits by-product N2O's
SCR reactors, which is characterized in that the distance between adjacent described diffuser branch pipe on each diffuser be 0.6m~
1m is 0.4m~0.6m preferably by the length for 0.7m~0.8m, each diffuser branch pipe.
8. raising low-temperature SCR catalyst according to any one of claim 1 to 6 is active and inhibits by-product N2O's
SCR reactors, which is characterized in that the diffusion hole the diffuser and it is described diffusion branch pipe on percent opening be 4%~
12%, preferably 5%~10%, are more selected as 7%~8%.
9. raising low-temperature SCR catalyst according to claim 8 is active and inhibits by-product N2The SCR reactors of O,
It is characterized in that, the aperture of each diffusion hole is 1mm~5mm, preferably 2mm~3mm.
10. raising low-temperature SCR catalyst according to claim 1 is active and inhibits by-product N2The SCR reactors of O,
It is characterized in that, deflector and flow straightening grid is equipped at the smoke inlet.
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| CN109499358A (en) * | 2018-12-26 | 2019-03-22 | 福建龙净脱硫脱硝工程有限公司 | Flue gas mixing heat riser and middle low temperature SCR denitration system |
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Application publication date: 20180727 |