CN109395585A - A kind of denitration reaction component for flue gas nitrogen oxide processing system - Google Patents
A kind of denitration reaction component for flue gas nitrogen oxide processing system Download PDFInfo
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- CN109395585A CN109395585A CN201810550166.9A CN201810550166A CN109395585A CN 109395585 A CN109395585 A CN 109395585A CN 201810550166 A CN201810550166 A CN 201810550166A CN 109395585 A CN109395585 A CN 109395585A
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 167
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 76
- 239000003546 flue gas Substances 0.000 title claims abstract description 61
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 238000012545 processing Methods 0.000 title claims description 46
- 239000003054 catalyst Substances 0.000 claims abstract description 151
- 239000007789 gas Substances 0.000 claims abstract description 26
- 239000006200 vaporizer Substances 0.000 claims abstract description 11
- 239000000428 dust Substances 0.000 claims description 41
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 27
- 230000008569 process Effects 0.000 claims description 24
- 229910052757 nitrogen Inorganic materials 0.000 claims description 14
- 238000007664 blowing Methods 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 7
- 230000001154 acute effect Effects 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 238000003860 storage Methods 0.000 claims description 2
- 230000007306 turnover Effects 0.000 claims 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 67
- 229910021529 ammonia Inorganic materials 0.000 abstract description 33
- -1 flue gas nitrogen oxides Chemical class 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 29
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 28
- 239000000908 ammonium hydroxide Substances 0.000 description 28
- 239000004568 cement Substances 0.000 description 26
- 238000009834 vaporization Methods 0.000 description 22
- 230000008016 vaporization Effects 0.000 description 22
- 229910001868 water Inorganic materials 0.000 description 16
- 239000000779 smoke Substances 0.000 description 15
- 230000000694 effects Effects 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 230000003749 cleanliness Effects 0.000 description 6
- 230000007613 environmental effect Effects 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- 235000019504 cigarettes Nutrition 0.000 description 5
- 238000009434 installation Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 238000010531 catalytic reduction reaction Methods 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 239000004744 fabric Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 238000013517 stratification Methods 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 230000007246 mechanism Effects 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010438 heat treatment Methods 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
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000009827 uniform distribution Methods 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
- B01D53/90—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
Landscapes
- 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
本发明提供一种应用于烟气氮氧化物高效处理设备技术领域的用于烟气氮氧化物处理系统的脱硝反应部件，用于烟气氮氧化物处理系统的脱硝反应部件的混合器(12)与汽化器(11)连通，混合器(12)同时与反应器(13)连通，反应器(13)内按间隙设置多个催化剂(5)，反应器(13)包括进气口(14)和排气口(15)，反应器(13)从进气口(14)一端到排气口(15)一端按间隙设置多个催化剂(5)，本发明所述的一种用于烟气氮氧化物处理系统的脱硝反应部件，确保汽化后的氨气与窑尾废气(工业烟气)充分混合，保证了氨与NOx的有效接触，在脱硝反应器内均匀分布，并在催化剂的作用下，快速反应，产生清洁的N2和H2O，提高烟气氮氧化物处理效率。
The present invention provides a denitration reaction component used in a flue gas nitrogen oxide treatment system and a mixer (12 ) is communicated with the vaporizer (11), the mixer (12) is communicated with the reactor (13) at the same time, a plurality of catalysts (5) are arranged in the reactor (13) according to the gap, and the reactor (13) includes an air inlet (14) and an exhaust port (15), the reactor (13) is provided with a plurality of catalysts (5) by gaps from one end of the air inlet (14) to one end of the exhaust port (15), and the one described in the present invention is used for flue gas The denitration reaction part of the nitrogen oxide treatment system ensures that the vaporized ammonia gas is fully mixed with the kiln tail gas (industrial flue gas), which ensures the effective contact between ammonia and NOx, and is evenly distributed in the denitration reactor. It can react quickly and generate clean N 2 and H 2 O, and improve the treatment efficiency of flue gas nitrogen oxides.
Description
Technical field
The invention belongs to flue gas nitrogen oxide efficient process equipment technical fields, are to be related to one kind to be used for more specifically
The denitration reaction component of flue gas nitrogen oxide processing system.
Background technique
In the prior art, pass through kiln tail discharge flue gas, and denitrating flue gas end-of-pipe control technology master when cement producing line produces
Will there are two types of, first, SNCR denitration technology (selective non-catalytic reduction technology)；Second, SCR denitration technology (selective catalysis
Reduction technique).SNCR denitration technology --- use ammonium hydroxide for reducing agent, no catalyst is needed in 850 DEG C or so lower and NOXInstead
It answers, realizes denitration.Therefore its reaction efficiency is lower, and denitration efficiency is only 60% or so, and reducing agent ammonium hydroxide consumption is big, discharge
Ammonia slip concentration is higher in tail gas, and there are secondary pollutions, more serious to the corrosion of remaining production equipment, increases plant maintenance
Cost, and there are biggish security risks.SCR denitration technology --- under dedicated catalyst action, using ammonium hydroxide as reducing agent,
Realize that denitrating flue gas is generally divided into high temperature modification, middle warm type and low form three types by catalyst reaction temperatures.High temperature modification SCR
Reaction temperature generally in 300~400 DEG C or so, the reaction temperature of middle warm type SCR generally in 180~250 DEG C or so, low form
The reaction temperature of SCR is generally at 100~150 DEG C or so.Because of the effect of catalyst, reaction efficiency is improved, denitration efficiency is reachable
90%.Only cement factory of the high temperature modification SCR in Europe has minimal amount of using achievement at present, and technical solution is still immature；In
Warm type SCR technology there is no in cement industry using achievement, need to solve dust concentration is big and denitration efficiency is low etc. in application process
Many technical problems.
Summary of the invention
The technical problems to be solved by the present invention are: it is simple to provide a kind of structure, industrial cigarette can be conveniently and efficiently realized
The hybrid reaction of gas and vaporization ammonia, it is ensured that the ammonia after vaporization is sufficiently mixed with kiln tail gas (industrial smoke), ensure that ammonia
With effectively contacting for NOx, makes the ammonia and NOx gas for being sufficiently mixed, contacting, be uniformly distributed in Benitration reactor, and be catalyzed
Under the action of agent, fast reaction generates clean N2And H2O, that improves flue gas nitrogen oxide treatment effeciency is used for flue gas nitrogen oxidation
The denitration reaction component of object processing system.
Solve the problems, such as techniques discussed above, the technical scheme adopted by the invention is as follows:
The present invention is a kind of denitration reaction component for flue gas nitrogen oxide processing system, and described is used for flue gas nitrogen oxygen
The denitration reaction component of compound processing system includes mixer and reactor, and mixer is connected to vaporizer, mixer simultaneously with
Reactor connection, presses the multiple catalyst of gap setting in reactor, and reactor includes air inlet and exhaust outlet, and reactor is from air inlet
The multiple catalyst of gap setting are pressed to exhaust outlet one end in mouth one end.
The denitration reaction component for flue gas nitrogen oxide processing system further includes deashing component, and deashing component is set
It sets in the reactor of denitration reaction component, the deashing component includes compressed-air atomizer, compressed air reservoir, blowing control
Component processed, each compressed-air atomizer pass through connecting line respectively and are connected to compressed air reservoir, be arranged on compressed air reservoir
Multiple compressions are arranged close to the position of each catalyst in the blowing control unit that compressed air start and stop and flow adjusting can be controlled
Air nozzle, the gas outlet close to multiple compressed-air atomizers of each catalyst are respectively aligned to the catalyst.
The denitration reaction component for flue gas nitrogen oxide processing system includes part case, mixer and reaction
Device is arranged in part case, and air inlet is arranged in reactor upper end, and exhaust outlet, catalyst and air inlet is arranged in reactor lower end
Between position ash slot is set, ash slot is connected to ash one end of the channel, the row of the ash channel other end and part case lower end
Grey mouth connection.
Catalyst includes first layer catalyst, second layer catalyst, third layer catalyst, and first layer catalyst is located at ash
Below slot, second layer catalyst is located at below first layer catalyst, and third layer catalyst is located at below second layer catalyst.
The ash channel is located at part case right positions, and multiple compressed airs are arranged in first layer catalyst left side
One or more compressed-air atomizers, each side of third layer catalyst is respectively set in nozzle, each side of second layer catalyst
One or more compressed-air atomizers are respectively set.
Multiple compressed-air atomizers of the first layer catalyst left side setting of the catalyst are horizontally disposed, each
Compressed-air atomizer is arranged vertically with first layer catalyst left side, and multiple compressed air sprays are arranged in second layer catalyst side
When mouth, air nozzle is partially compressed and is arranged vertically with second layer catalyst side, air nozzle is partially compressed and the second layer is catalyzed
Agent side angle arrangement at an acute angle, when multiple compressed-air atomizers are arranged in third layer catalyst side, is partially compressed air nozzle
It is arranged vertically with third layer catalyst side, air nozzle is partially compressed and third layer catalyst side angle at an acute angle is arranged.
Weight turning plate valve is set on the ash channel, and the dust that ash slot is transported to ash channel is configured to
Under fall on the structure on weight turning plate valve, the dust whereabouts that ash slot is transported to ash channel is stacked on weight turning plate valve
Actual weight be more than weight turning plate valve setting weight numerical value when, weight turning plate valve is configured to open, so that heap
Dust of the product on weight turning plate valve can fall on down the structure of ash discharging hole discharge.
Using technical solution of the present invention, can obtain it is below the utility model has the advantages that
Flue gas nitrogen oxide processing system of the present invention is needing to handle the nitrogen oxides in industrial smoke
When, flue gas nitrogen oxide processing system of the present invention is added, flue gas nitrogen oxide processing system is arranged in cement producing line
Kiln tail high-temperature blower and raw material mill between position, the flue gas of kiln tail discharge leads to denitration reaction component, and ammonium hydroxide vaporization portion
Part handles ammonium hydroxide, so that ammonium hydroxide vaporizes, the ammonium hydroxide then vaporized also enters denitration reaction component, the ammonia of flue gas and vaporization
Water mixes in denitration reaction component, is then reacted again under the effect of the catalyst.In this way, in the ammonium hydroxide and flue gas of vaporization
Nitrogen oxides accelerate effectively mixing, and react, to be converted to the nitrogen and water of cleanliness without any pollution, nitrogen and water from de-
The discharge of nitre reaction part, and the original process system of cement producing line is returned to, it is discharged after dust removal process by kiln tail chimney.The present invention
The processing system, for handling the kiln tail gas containing high concentrate NOx discharged in clinker production process.By deeply
Nitrogen oxides mechanism of production in clinker production process of analyzing and researching, in the technological process of production each position smoke property, cigarette
Dust physics and chemical characteristic and the denitration reaction principles of chemistry in gas, the present invention is by selective catalytic reduction reaction technology and cement
Plant production processes process deeply merges, and it is stifled to solve catalyst existing for middling temperature DeNOx under the conditions of 180~220 DEG C of temperature
The uneven technical problems such as low with denitration efficiency of plug, gas mixing.It is of the present invention a kind of for flue gas nitrogen oxide processing system
The denitration reaction component of system, structure is simple, can conveniently and efficiently realize industrial smoke and vaporize the hybrid reaction of ammonia, it is ensured that
Ammonia after vaporization is sufficiently mixed with kiln tail gas (industrial smoke), ensure that effectively contacting for ammonia and NOx, make to be sufficiently mixed,
The ammonia and NOx gas of contact, are uniformly distributed, and under the effect of the catalyst, fast reaction in Benitration reactor, generate cleaning
N2And H2O improves flue gas nitrogen oxide treatment effeciency.
Detailed description of the invention
Brief description is made to content expressed by each attached drawing of this specification and the label in figure below:
Fig. 1 is the overall structure diagram of flue gas nitrogen oxide processing system of the present invention；
Fig. 2 is the structural schematic diagram of the reactor of denitration reaction component of the present invention；
Fig. 3 is the compressed-air atomizer cloth of the first layer catalyst of the deashing component of denitration reaction component of the present invention
Set signal figure structure schematic representation；
Fig. 4 is the compressed-air atomizer cloth of the second layer catalyst of the deashing component of denitration reaction component of the present invention
Set signal figure structure schematic representation；
Fig. 5 is the compressed-air atomizer cloth of the third layer catalyst of the deashing component of denitration reaction component of the present invention
Set signal figure structure schematic representation；
Attached drawing acceptance of the bid note is respectively as follows: 1, ammonium hydroxide vaporization member；2, denitration reaction component；3, cement producing line；4, kiln tail；5,
Catalyst；6, tank used for storing ammonia；7, air compressor；8, air accumulator；9, centrifugal blower；10, air heater；11, vaporizer；
12, mixer；13, reactor；14, air inlet；15, exhaust outlet；16, deashing component；17, compressed-air atomizer；18, compression is empty
Gas storage tank；19, it is blown control unit；22, atomizer；24, part case；25, ash slot；26, ash channel；27, ash discharging hole；
28, first layer catalyst；29, second layer catalyst；30, third layer catalyst；31, weight turning plate valve；32, preparing catalyst
Installation site；33, absorption type dryer.
Specific embodiment
Below against attached drawing, by the description of the embodiment, to for example related each structure of a specific embodiment of the invention
The works such as the shape of part, construction, the mutual alignment between each section and connection relationship, the effect of each section and working principle are further
Detailed description:
As shown in attached drawing 1- attached drawing 5, the present invention is a kind of flue gas nitrogen oxide processing system, the flue gas nitrogen oxide
Processing system includes ammonium hydroxide vaporization member 1, denitration reaction component 2, the kiln of the denitration reaction component 2 and cement producing line 3
Tail 4 is connected to, and denitration reaction component 2 is connected to ammonium hydroxide vaporization member 1 simultaneously, the multiple catalyst 5 of setting in desulphurization reaction component 2,
The material of catalyst 5 is the inorganic material of low temperature calcination.Above structure is being needed at the nitrogen oxides in industrial smoke
When reason, flue gas nitrogen oxide processing system of the present invention is added, flue gas nitrogen oxide processing system is arranged in manufacture of cement
The flue gas (including oxynitrides) of position between high-temperature blower and the raw material mill of the kiln tail of line, kiln tail discharge leads to denitration reaction
Component 2, and ammonium hydroxide vaporization member 1 handles ammonium hydroxide, so that ammonium hydroxide vaporizes, the ammonium hydroxide then vaporized also enters denitration reaction
The ammonium hydroxide of component 2, flue gas and vaporization mixes in denitration reaction component 2, is then reacted again under the effect of the catalyst.This
Sample, the nitrogen oxides in the nitrogen and flue gas of vaporization accelerates effectively mixing, and reacts, to be converted to cleanliness without any pollution
Nitrogen and water, nitrogen and water are discharged from denitration reaction component 2, and return to the original process system of cement producing line, through dust removal process
It is discharged afterwards by kiln tail chimney.Processing system of the present invention, for handle discharged in clinker production process containing highly concentrated
Spend the kiln tail gas of NOx.By analysing in depth nitrogen oxides mechanism of production, production technology stream in research clinker production process
Dust physics and chemical characteristic and the denitration reaction principles of chemistry, the present invention will select in the smoke property, flue gas at each position in journey
Property catalytic reduction reaction technology is deeply merged with cement factory production process, is solved under the conditions of 180~220 DEG C of temperature
The uneven technical problems such as low with denitration efficiency of catalyst blockage existing for warm SCR denitration, gas mixing.Flue gas of the present invention
Nitrogen oxides treatment system, structure is simple, at low cost, can easily and efficiently be used for the conversion of nitrogen oxides in industrial smoke
It for the nitrogen and water of cleanliness without any pollution, is discharged in whole process without waste water and waste liquid, process safety environmental protection, it is possible to reduce nitrogen oxidation
Pollution of the object to environment, facilitate promoted cement industry level of clean production, thus reduce cement factory NOx emission concentration,
It reduces denitration ammonia volume, reduce corrosion of the system the escaping of ammonia to equipment and the secondary pollution to environment.
Flue gas nitrogen oxide processing system of the present invention, from energy conservation and environmental protection, the angle of green production, for water
The process characteristic of mud sinter leaching system studies the middle warm type SCR denitration technology for being suitble to cement industry to use, to further decrease
Cement factory NOx emission concentration reduces denitration ammonia volume, reduces system the escaping of ammonia to the corrosion of equipment and to the secondary of environment
Pollution.Processing system of the invention can be applied to the processing of cement clinker production line kiln tail gas, in the existing production work of production line
This system is added in skill process, only needs the short-term kiln that stops that the construction working of system interface can be completed during implementation, to original life
The influence of production system is smaller.Processing system of the invention is used to the conversion of nitrogen oxides in industrial smoke be cleanliness without any pollution
Nitrogen and water are discharged in whole process without waste water and waste liquid, process safety environmental protection, it is possible to reduce dirt of the nitrogen oxides to environment
Dye facilitates the level of clean production for further promoting cement industry, reduces cost, realize environmental protection.
Flue gas nitrogen oxide processing system of the present invention, (1) do not influence cement producing line and normally produce.Of the invention
Processing system is mainly arranged between the existing kiln tail high-temperature blower of production line and raw material mill, is located at after afterheat generating system, cigarette
About 180~220 DEG C of temperature degree, air quantity and temperature before and after fume treatment are basically unchanged, will not be to the quality of cement producing line
It is had an impact with matched raw material grinding and afterheat generating system, the fluctuation of operating condition will not be caused.(2) dust is adaptable.It adopts
With compressed air spraying formula deashing component, the mating dedicated compressed air system of setting and blowing spray head ensure that the steady of gas source
It is qualitative, improve blowing effect.And by the way that compressed air spraying position, the blowing frequency and bleed pressure is rationally arranged, guarantee high
Catalyst pores are not plugged up under dust concentration.(3) denitration efficiency is high.Using ammonium hydroxide vaporization member, ammonia and NOx are substantially increased
Reactivity, be conducive to ammonia and the fast reaction of NOx；Using efficient mixer, ammonia and kiln tail gas after making vaporization
(industrial smoke) is sufficiently mixed, and ensure that ammonia is contacted with the effective of NOx；Using airflow uniform distribution formula Benitration reactor, make sufficiently mixed
It closes, the ammonia and NOx gas of contact, is uniformly distributed in Benitration reactor, and under the effect of the catalyst, fast reaction, generated
Clean N2And H2O effectively improves efficiency.
The ammonium hydroxide vaporization member 1 adds including tank used for storing ammonia 6, air compressor 7, air accumulator 8, centrifugal blower 9, air
Hot device 10, vaporizer 11, air accumulator 8 are connected to air compressor 7 and vaporizer 11 respectively, air compressor 7 and tank used for storing ammonia 6
Connection, air heater 10 are connected to centrifugal blower 9 and vaporizer 11 respectively, and vaporizer 11 is connected to denitration reaction component 2.Institute
The ammonium hydroxide vaporization member 1 stated further includes absorption type dryer 33, and 33 one end of absorption type dryer is connected to air compressor 7, is inhaled
Attached 33 other end of formula drier is connected to air accumulator 8.Above structure can efficiently be handled ammonium hydroxide, so that ammonium hydroxide becomes
The vaporization ammonia needed, to accelerate in ammonia and industrial smoke in denitration reaction component 2 with industrial oxygen effecting reaction
The reaction speed of oxynitrides improves nitrogen oxides treatment effect, improves efficiency.
The denitration reaction component 2 (the denitration reaction component for flue gas nitrogen oxide processing system) includes mixer
12 and reactor 13, the mixer 12 be connected to vaporizer 11, mixer 12 is connected to reactor 13 simultaneously, reactor 13
Interior to press the multiple catalyst 5 of gap setting, the reactor 13 includes air inlet 14 and exhaust outlet 15, and reactor 13 is from air inlet
The multiple catalyst 5 of gap setting are pressed to 15 one end of exhaust outlet in 14 one end.Above structure, the mixer of denitration reaction component 2 are set
It sets, so that industrial smoke and vaporization ammonia enter mixer simultaneously, carries out mixed at high speed, form mixed flue gas, then mix cigarette
Gas enters back into reactor and is reacted, and is decomposed into clean nitrogen and water in the reactor, it is original to be then return to cement producing line
Process system is discharged after dust removal process by kiln tail chimney.
The flue gas nitrogen oxide processing system further includes deashing component 16, and deashing component 16 is arranged in denitration reaction portion
In part 2, the deashing component 16 includes compressed-air atomizer 17, compressed air reservoir 18, blowing control unit 19, each pressure
Contracting air nozzle 17 is connected to by connecting line with compressed air reservoir 18 respectively, and setting can control on compressed air reservoir 18
Multiple compressed airs are arranged close to the position of each catalyst 5 in the blowing control unit 19 that compressed air start and stop and flow are adjusted
Nozzle 17, the gas outlet close to multiple compressed-air atomizers 17 of each catalyst 5 are respectively aligned to the catalyst 5.Above structure,
Denitration reaction component 2 after a period of use during, surface can accumulate a large amount of dust in catalyst therein, dusty dense
Spending lower catalyst pores can be blocked, and influence the reflection effect of catalyst.In order to solve this problem, the present invention designs deashing component
16, processing system after a period of use, according to the program set automatically to catalyst carry out deashing processing.At this moment, it needs
It first to shut down, the switch of solenoid valve is then controlled by PLC, and then control compressed-air atomizer and spray compressed air, compression is empty
The dust accumulated on catalyst is blown disengaging catalyst by gas, realizes the automatic cleaning of catalyst.In this way, can not only guarantee to locate
Reason system can keep efficient process state constantly, and deashing does not need to dismantle denitration reaction component 2, and labor intensity is low, clearly
Ash is high-efficient.
The vaporizer 11 includes atomizer 22 and gasifier 23, and 22 one end of atomizer is connected to air accumulator 8, atomizer
22 other ends are connected to gasifier 23, and air heater 10 is connected to gasifier 23, gasifier 23 simultaneously with denitration reaction component 2
Mixer 12 be connected to.Above structure, the effect of vaporizer are to mix to the air after ammonium hydroxide and heating, so that ammonium hydroxide
It is effectively mixed with after air heating, forms atomization ammonia, the mixer for entering denitration reaction component 2 is then sprayed from gasifier,
Ammonia and being sufficiently mixed in a mixer in oxygen to nitrogen oxides are vaporized, mixed flue gas is formed, it is fast then to enter reactor
Speed reaction.
The catalyst 5 includes first layer catalyst 28, second layer catalyst 29, third layer catalyst 30, described
First layer catalyst 28 is located at 25 lower position of ash slot, and second layer catalyst 29 is located at 28 lower position of first layer catalyst,
Third layer catalyst 30 is located at 29 lower position of second layer catalyst.Above structure, by the setting of three catalyst, and it is different
Catalyst from air inlet to exhaust outlet extend, in this way, through mixer outflow flue gas, vaporization the mixed mixed flue gas of ammonia into
After entering reactor, multiple tracks successively can be carried out by first layer catalyst 28, second layer catalyst 29, third layer catalyst 30 and urged
Change.
The horizontal cloth of multiple compressed-air atomizers 17 of 28 left side of the first layer catalyst setting of the catalyst 5
It sets, each compressed-air atomizer 17 is arranged vertically with 28 left side of first layer catalyst, above structure, multiple compressed air sprays
Mouth can reliably blow off the dust accumulated on first layer catalyst first layer catalyst, so that dust enters ash slot, then
From the flowing of ash channel 26, collect, discharge.When multiple compressed-air atomizers 17 are arranged in 29 side of second layer catalyst, part is pressed
Contracting air nozzle 17 is arranged vertically with 29 side of second layer catalyst, and air nozzle 17 and 29 side of second layer catalyst is partially compressed
Face angle arrangement at an acute angle, above structure, the dust that multiple compressed-air atomizers will reliably can be accumulated on second layer catalyst
Blow off second layer catalyst, and when multiple compressed-air atomizers 17 are arranged in 30 side of third layer catalyst, air nozzle is partially compressed
17 are arranged vertically with 30 side of third layer catalyst, and air nozzle 17 and 30 side of third layer catalyst folder at an acute angle is partially compressed
Angle arrangement.Above structure, multiple compressed-air atomizers can reliably blow off the dust accumulated on third layer catalyst third layer
Catalyst.Because three catalyst are arranged, first layer catalyst, which can adsorb, stops a large amount of dust, and first layer catalyst is accumulation
Dust is most, therefore, it is desirable to which the compressed-air atomizer being arranged on first layer catalyst blows off the dust on the first catalyst converter
First catalyst converter, and to be recycled by ash slot and ash channel.And after first layer catalyst, fall on the second layer
Dust on catalyst and third layer catalyst is less, therefore it may only be necessary to which dust is blown off by respective compressed-air atomizer
Catalyst converter, in this way, reliably realizing deashing processing.
The ash channel 26 is located at 25 lower position of ash slot, and multiple compressions are arranged in 28 left side of first layer catalyst
One or more compressed-air atomizers 17, third layer catalysis is respectively set in air nozzle 17, each side of second layer catalyst 29
One or more compressed-air atomizers 17 are respectively set in each side of agent 30.Above structure, it is a certain amount of in catalyst buildup
After dust, dust can have an adverse effect to the trafficability performance of catalyst, at this moment, be blown control unit by starting, control is not
Compressed air, which is sprayed, with the compressed-air atomizer being arranged on catalyst carries out soot blowing.After the starting of multiple compressed-air atomizers, the
Compressed-air atomizer on one layer of catalyst acts on first layer catalyst, blow dust on first layer catalyst it is mobile from
First layer catalyst is opened, to generate flow-disturbing, dust flows to ash slot 25, realize the soot blowing cleaning of first layer catalyst, and flow
It will continue to flow to the dust of ash slot, be accumulated until flowing to ash channel 26, is then periodically discharged from ash discharging hole.
Weight turning plate valve 31 is set on the ash channel 26, and the dust that ash slot 25 is transported to ash channel 26 is set
It is set to the structure that can be fallen on down on weight turning plate valve 31, the dust whereabouts that ash slot 25 is transported to ash channel 26 is stacked into
When actual weight on weight turning plate valve 31 is more than the setting weight numerical value of weight turning plate valve 18, weight turning plate valve 31 is set
Being set to can open, and enable the structure that the discharge of ash discharging hole 27 is fallen under the dust being deposited on weight turning plate valve 31.On
Structure is stated, after ash slot 25 collects the dust stratification of first layer catalyst, dust stratification can fall from ash channel 26, fall on weight flap valve
On door 31.When the actual weight that the dust whereabouts for being transported to ash channel 26 from ash slot 25 is stacked on weight turning plate valve 31
Less than weight turning plate valve 18 setting weight numerical value when, weight turning plate valve 31 will not be opened, and dust stratification is persistently saved bit by bit.And when product
When grey actual weight is more than the setting weight numerical value of weight turning plate valve 18, weight turning plate valve 31 can be opened, so that accumulation
Dust on weight turning plate valve 31 can fall on down the discharge of ash discharging hole 27, reliably realize periodic cleaning and the row of dust stratification in this way
Out, it is ensured that processing system function is unaffected.
The catalyst 5 further includes preparing catalyst installation site 32, and the setting of preparing catalyst installation site 32 is the
The portion of 32 lower position of preparing catalyst installation site is arranged in three layers of 30 lower position of catalyst, the exhaust outlet 15 of reactor 13
On part shell 24.Above structure, 32 position of preparing catalyst installation site can install preparing catalyst.When three first layers catalyst
Performance with using accumulated time and declining to a certain extent when, one layer of catalyst therein can be moved to spare level, and
New catalyst is put into raw catalyst layer.In addition, production line biggish for fluctuation of operating conditions, spare level can also be used, one
4 layers of catalyst of secondary loading, to guarantee the discharge standard of meet the requirement of environmental protection.
Flue gas nitrogen oxide processing system of the invention carries out small-scale examination experiment, actual measurement in certain cement clinker production line
For denitration efficiency 90%~95%, the escaping of ammonia is not detected in 500~800Pa of system resistance, all indicators are better than existing SNCR and
High temperature SCR denitration technology, therefore, the present invention can effectively improve treatment effect.
Flue gas nitrogen oxide processing system of the present invention is needing to handle the nitrogen oxides in industrial smoke
When, flue gas nitrogen oxide processing system of the present invention is added, flue gas nitrogen oxide processing system is arranged in cement producing line
Kiln tail high-temperature blower and raw material mill between position, the flue gas of kiln tail discharge leads to denitration reaction component, and ammonium hydroxide vaporization portion
Part handles ammonium hydroxide, so that ammonium hydroxide vaporizes, the ammonium hydroxide then vaporized also enters denitration reaction component, the ammonia of flue gas and vaporization
Water mixes in denitration reaction component, is then reacted again under the effect of the catalyst.In this way, in the ammonium hydroxide and flue gas of vaporization
Nitrogen oxides accelerate effectively mixing, and react, to be converted to the nitrogen and water of cleanliness without any pollution, nitrogen and water from de-
The discharge of nitre reaction part, and the original process system of cement producing line is returned to, it is discharged after dust removal process by kiln tail chimney.The present invention
The processing system, for handling the kiln tail gas containing high concentrate NOx discharged in clinker production process.By deeply
Nitrogen oxides mechanism of production in clinker production process of analyzing and researching, in the technological process of production each position smoke property, cigarette
Dust physics and chemical characteristic and the denitration reaction principles of chemistry in gas, the present invention is by selective catalytic reduction reaction technology and cement
Plant production processes process deeply merges, and it is stifled to solve catalyst existing for middling temperature DeNOx under the conditions of 180~220 DEG C of temperature
The uneven technical problems such as low with denitration efficiency of plug, gas mixing.Flue gas nitrogen oxide processing system of the present invention, structure letter
Single, manufacturing cost is low, can easily and efficiently be used for the nitrogen by the conversion of nitrogen oxides in industrial smoke for cleanliness without any pollution
And water, it is discharged without waste water and waste liquid in whole process, process safety environmental protection, it is possible to reduce pollution of the nitrogen oxides to environment has
Help promoted cement industry level of clean production, thus reduce cement factory NOx emission concentration, reduce denitration ammonia volume,
Corrosion of the reduction system the escaping of ammonia to equipment and the secondary pollution to environment.
Above in conjunction with attached drawing, an exemplary description of the invention, it is clear that concrete implementation of the present invention is not by above-mentioned
The limitation of mode, as long as using the various improvement that the inventive concept and technical scheme of the present invention carry out, or not improved by this
The conception and technical scheme of invention directly apply to other occasions, are within the scope of the invention.
Claims (7)
1. a kind of denitration reaction component for flue gas nitrogen oxide processing system, it is characterised in that: described is used for flue gas nitrogen
The denitration reaction component of oxide process system includes mixer (12) and reactor (13), mixer (12) and vaporizer (11)
Connection, mixer (12) are connected to reactor (13) simultaneously, and the multiple catalyst of gap setting (5), reaction are pressed in reactor (13)
Device (13) includes air inlet (14) and exhaust outlet (15), and reactor (13) is pressed from air inlet (14) one end to exhaust outlet (15) one end
The multiple catalyst of gap setting (5).
2. the denitration reaction component according to claim 1 for flue gas nitrogen oxide processing system, it is characterised in that: institute
The denitration reaction component for flue gas nitrogen oxide processing system stated further includes deashing component (16), deashing component (16) setting
In the reactor (13) of denitration reaction component (2), the deashing component (16) includes compressed-air atomizer (17), compression sky
Gas storage tank (18), blowing control unit (19), each compressed-air atomizer (17) are stored up by connecting line and compressed air respectively
Tank (18) is connected to, the blowing control unit that setting can control compressed air start and stop on compressed air reservoir (18) and flow is adjusted
(19), multiple compressed-air atomizers (17) are arranged in the position close to each catalyst (5), close to the multiple of each catalyst (5)
The gas outlet of compressed-air atomizer (17) is respectively aligned to the catalyst (5).
3. the denitration reaction component according to claim 1 or 2 for flue gas nitrogen oxide processing system, feature exist
In: the denitration reaction component for flue gas nitrogen oxide processing system include part case (24), mixer (12) and
Reactor (13) is arranged in part case (24), and air inlet (14) are arranged in reactor (13) upper end, reactor (13) lower end
It is arranged exhaust outlet (15), position setting ash slot (25) between catalyst (5) and air inlet (14), ash slot (25) and ash are logical
The connection of road (26) one end, ash channel (26) other end are connected to the ash discharging hole (27) of part case (24) lower end.
4. the denitration reaction component according to claim 1 or 2 for flue gas nitrogen oxide processing system, feature exist
In: the catalyst (5) include first layer catalyst (28), second layer catalyst (29), third layer catalyst (30), first
Layer catalyst (28) is located at below ash slot (25), and second layer catalyst (29) is located at below first layer catalyst (28), third
Layer catalyst (30) is located at below second layer catalyst (29).
5. the denitration reaction component according to claim 3 for flue gas nitrogen oxide processing system, it is characterised in that: institute
The ash channel (26) stated is located at ash slot (25) lower position, and multiple compressed airs are arranged in first layer catalyst (28) left side
One or more compressed-air atomizers (17) are respectively set in nozzle (17), second layer catalyst (29) each side, and third layer is urged
One or more compressed-air atomizers (17) are respectively set in agent (30) each side.
6. the denitration reaction component according to claim 4 for flue gas nitrogen oxide processing system, it is characterised in that: institute
Multiple compressed-air atomizers (17) of first layer catalyst (28) the left side setting for the catalyst (5) stated are horizontally disposed, often
A compressed-air atomizer (17) is arranged vertically with first layer catalyst (28) left side, the setting of second layer catalyst (29) side
When multiple compressed-air atomizer (17), air nozzle (17) are partially compressed and are arranged vertically with second layer catalyst (29) side, portion
Partial compression air nozzle (17) and second layer catalyst (29) side angle at an acute angle arrange that third layer catalyst (30) side is set
When setting multiple compressed-air atomizers (17), air nozzle (17) are partially compressed and are arranged vertically with third layer catalyst (30) side,
Air nozzle (17) and third layer catalyst (30) side angle at an acute angle is partially compressed to arrange.
7. the denitration reaction component according to claim 3 for flue gas nitrogen oxide processing system, it is characterised in that: institute
Weight turning plate valve (31) are set on the ash channel (26) stated, ash slot (25) is transported to the dust setting in ash channel (26)
For the structure that can be fallen on down on weight turning plate valve (31), ash slot (25) is transported to the dust whereabouts heap in ash channel (26)
When actual weight in product to weight turning plate valve (31) is more than the setting weight numerical value of weight turning plate valve (18), weight turnover panel
Valve (31) is configured to open, and enables and falls on ash discharging hole (27) under the dust being deposited on weight turning plate valve (31)
The structure of discharge.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111229031A (en) * | 2020-03-03 | 2020-06-05 | 安徽海螺建材设计研究院有限责任公司 | A dust removal system and a dust removal method therefor |
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Effective date of registration: 20190604 Address after: No. 39 Cultural Road, Jinghu District, Wuhu City, Anhui Province, 241000 Applicant after: ANHUI CONCH GROUP Co.,Ltd. Applicant after: ANHUI CONCH DESIGN & RESEARCH INSTITUTE OF BUILDING MATERIALS Co.,Ltd. Applicant after: ANHUI CONCH CEMENT Co.,Ltd. Address before: 241000 South Jiuhua Road 1017, Yijiang District, Wuhu City, Anhui Province Applicant before: ANHUI CONCH DESIGN & RESEARCH INSTITUTE OF BUILDING MATERIALS Co.,Ltd. |
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Application publication date: 20190301 |