CN109731462A - A flue gas nitrogen oxide treatment system - Google Patents
A flue gas nitrogen oxide treatment system Download PDFInfo
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- CN109731462A CN109731462A CN201810551170.7A CN201810551170A CN109731462A CN 109731462 A CN109731462 A CN 109731462A CN 201810551170 A CN201810551170 A CN 201810551170A CN 109731462 A CN109731462 A CN 109731462A
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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烟气氮氧化物处理系统，所述的烟气氮氧化物处理系统的脱硝反应部件(2)与水泥生产线(3)的窑尾(4)连通，脱硝反应部件(2)同时与氨水汽化部件(1)连通，脱硫反应部件(2)内设置多个催化剂(5)，催化剂(5)的材料为低温煅烧的无机材料，本发明所述的烟气氮氧化物处理系统，结构简单，制造成本低，能够方便高效地用于将工业烟气中的氮氧化物转化为清洁无污染的氮气和水，整个过程中无废水和废液排出，过程安全环保，可以减少氮氧化物对环境的污染，有助于提升水泥行业的清洁生产水平，从而降低水泥工厂NOx排放浓度、降低脱硝氨水用量。
The present invention provides a flue gas nitrogen oxide treatment system applied in the technical field of flue gas nitrogen oxide high-efficiency treatment equipment. The denitration reaction component (2) of the flue gas nitrogen oxide treatment system and the cement production line (3) The kiln tail (4) is connected, the denitration reaction part (2) is connected with the ammonia water vaporization part (1) at the same time, a plurality of catalysts (5) are arranged in the desulfurization reaction part (2), and the material of the catalyst (5) is an inorganic material calcined at low temperature , The flue gas nitrogen oxide treatment system of the present invention has simple structure and low manufacturing cost, and can be conveniently and efficiently used to convert nitrogen oxides in industrial flue gas into clean and pollution-free nitrogen and water. The discharge of waste water and waste liquid is safe and environmentally friendly, which can reduce the pollution of nitrogen oxides to the environment, and help to improve the level of clean production in the cement industry, thereby reducing the concentration of NOx emissions in cement plants and the consumption of denitrifying ammonia water.
Description
Technical field
The invention belongs to flue gas nitrogen oxide efficient process equipment technical fields, are to be related to a kind of flue gas more specifically
Nitrogen oxides treatment 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: providing, a kind of structure is simple, and can easily and efficiently be used for will be industrial
Conversion of nitrogen oxides in flue gas is the nitrogen and water of cleanliness without any pollution, is discharged in whole process without waste water and waste liquid, process peace
Loopful is protected, it is possible to reduce pollution of the nitrogen oxides to environment facilitates the level of clean production for promoting cement industry, to reduce
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 atmosphere
The flue gas nitrogen oxide processing system of pollution.
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 flue gas nitrogen oxide processing system, and the flue gas nitrogen oxide processing system includes ammonium hydroxide vapour
Change component, denitration reaction component, the denitration reaction component is connected to the kiln tail of cement producing line, and denitration reaction component is simultaneously
It is connected to ammonium hydroxide vaporization member, the multiple catalyst of setting in desulphurization reaction component, the material of catalyst is the inorganic of low temperature calcination
Material.
The ammonium hydroxide vaporization member include tank used for storing ammonia, air compressor, air accumulator, centrifugal blower, air heater,
Vaporizer, air accumulator are connected to air compressor and vaporizer respectively, and air compressor is connected to tank used for storing ammonia, air heater
It is connected to respectively with centrifugal blower and vaporizer, vaporizer and denitration reaction members.
The ammonium hydroxide vaporization member further includes absorption type dryer, and absorption type dryer one end and air compressor connect
Logical, the absorption type dryer other end is connected to air accumulator.
The denitration reaction component includes mixer and reactor, and mixer is connected to vaporizer, mixer simultaneously with
Reactor connection, reactor is interior to press the multiple catalyst of gap setting, and the reactor includes air inlet and exhaust outlet, reactor
The multiple catalyst of gap setting are pressed from air inlet one end to exhaust outlet one end.
The flue gas nitrogen oxide processing system further includes deashing component, and deashing component is arranged in denitration reaction component
Interior, the deashing component includes compressed-air atomizer, compressed air reservoir, blowing control unit, each compressed-air atomizer
It is connected to respectively by connecting line with compressed air reservoir, setting can control compressed air start and stop and stream on compressed air reservoir
The blowing control unit adjusted is measured, multiple compressed-air atomizers are set close to the position of each catalyst, close to each catalyst
The gas outlets of multiple compressed-air atomizers be respectively aligned to the catalyst.
The reactor lower end position of the denitration reaction component also sets up nitrogen outlet and water outlet, nitrogen discharge
Mouth is connected to nitrogen recycling tank, and water outlet is connected to water recovery tank.
The vaporizer includes atomizer and gasifier, and atomizer one end is connected to air accumulator, the atomizer other end with
Gasifier connection, air heater are connected to gasifier, and gasifier is connected to the mixer of denitration reaction component simultaneously.
The denitration reaction component includes part case, and mixer and reactor are arranged in part case, reaction
Air inlet is arranged in device upper end, and exhaust outlet is arranged in reactor lower end, and ash slot, ash slot is arranged in position between catalyst and air inlet
It is connected to ash one end of the channel, the ash channel other end is connected to the ash discharging hole of part case lower end.
The catalyst includes first layer catalyst, second layer catalyst, third layer catalyst, and the first layer is urged
Agent is located at the upper position of reactor inner space, and second layer catalyst is located at first layer catalyst lower position, third layer
Catalyst is located at second layer catalyst lower position.
The ash channel is located at ash slot lower position, and multiple compressed air sprays are arranged in first layer catalyst left side
One or more compressed-air atomizers, each side of third layer catalyst point is respectively set in mouth, each side of second layer catalyst
It She Zhi not one or more compressed-air atomizers.
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.
The catalyst further includes preparing catalyst installation site, and the setting of preparing catalyst installation site is urged in third layer
Agent lower position, the exhaust outlet of reactor are arranged on the part case of preparing catalyst installation site lower position.
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.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.
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 includes mixer 12 and reactor 13, and mixer 12 is connected to vaporizer 11, is mixed
Device 12 is connected to reactor 13 simultaneously, and the multiple catalyst 5 of gap setting are pressed in reactor 13, and the reactor 13 includes air inlet
Mouth 14 and exhaust outlet 15, reactor 13 press the multiple catalyst 5 of gap setting from 14 one end of air inlet to 15 one end of exhaust outlet.It is above-mentioned
Structure, the setting of mixer, industrial smoke and vaporization ammonia enter mixer simultaneously, carry out mixed at high speed, form mixed flue gas,
Then mixed flue gas enters back into reactor and is reacted, and is decomposed into clean nitrogen and water in the reactor, is then return to cement
The original process system of production line, 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 denitration reaction component 2 includes part case 24, and mixer 12 and reactor 13 are arranged at part case
In 24, air inlet 14 is arranged in 13 upper end of reactor, and exhaust outlet 15 is arranged in 13 lower end of reactor, between catalyst 5 and air inlet 14
Ash slot 25 is arranged in position, and ash slot 25 is connected to 26 one end of ash channel, under 26 other end of ash channel and part case 24
The ash discharging hole 27 at end is connected to.
The catalyst 5 includes first layer catalyst 28, second layer catalyst 29, third layer catalyst 30, and described the
One layer of catalyst 28 is located at the upper position of reactor inner space, and second layer catalyst 29 is located at 28 lower section of first layer catalyst
Position, third layer catalyst 30 are located at 29 lower position of second layer catalyst.Above structure, by the setting of three layers of catalyst,
And different catalysts extend from air inlet to exhaust outlet, in this way, the flue gas through mixer outflow, the vaporization mixed mixing of ammonia
After flue gas enters reactor, can successively it be carried out by first layer catalyst 28, second layer catalyst 29, third layer catalyst 30 more
Road catalysis.
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 layers of 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 the dust on first layer catalyst converter
From first layer catalyst converter, and to be discharged 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 24 right positions of part case, and multiple pressures are arranged in 28 left side of first layer catalyst
One or more compressed-air atomizers 17 are respectively set in contracting air nozzle 17, each side of second layer catalyst 29, and third layer is urged
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
Dust after, dust can have an adverse effect to the trafficability performance of catalyst, at this moment, pass through starting blowing control unit, control
The compressed-air atomizer being arranged in different catalysts sprays compressed air and carries out soot blowing.After the starting of multiple compressed-air atomizers,
Compressed-air atomizer on first layer catalyst acts on first layer catalyst, and the dust blown on first layer catalyst is mobile
First layer catalyst is left, to generate flow-disturbing, dust flows to ash slot 25, realize the soot blowing cleaning of first layer catalyst, and
The dust for flowing to ash slot will continue to flow, and be accumulated until flowing to ash channel 26, then periodically be 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 flap gate 31, 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 31 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 31, 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 nitrogen 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, is then return to the original process system of cement producing line, is discharged after dust removal process by kiln tail chimney.This hair
The bright processing system, for handling the kiln tail gas containing high concentrate NOx discharged in clinker production process.Pass through depth
Enter to analyze and research nitrogen oxides mechanism of production in clinker production process, the smoke property at each position in the technological process of production,
Dust physics and chemical characteristic and the denitration reaction principles of chemistry in flue gas, the present invention is by selective catalytic reduction reaction technology and water
Bricklayer's factory production process deeply merges, and solves 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 blocking, gas mixing.Flue gas nitrogen oxide processing system of the present invention, structure
Simply, 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
Gas and water are discharged in whole process without waste water and waste liquid, process safety environmental protection, it is possible to reduce pollution of the nitrogen oxides to environment,
Facilitate the level of clean production of promotion cement industry, to reduce cement factory NOx emission concentration, reduce denitration ammonium hydroxide use
Amount reduces corrosion of the 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 (10)
1. a kind of flue gas nitrogen oxide processing system, it is characterised in that: the flue gas nitrogen oxide processing system includes ammonium hydroxide
Vaporization member (1), denitration reaction component (2), the denitration reaction component (2) and the kiln tail (4) of cement producing line (3) connect
Logical, denitration reaction component (2) is connected to ammonium hydroxide vaporization member (1) simultaneously, the multiple catalyst of setting in desulphurization reaction component (2)
(5), the material of catalyst (5) is the inorganic material of low temperature calcination.
2. flue gas nitrogen oxide processing system according to claim 1, it is characterised in that: the ammonium hydroxide vaporization member
It (1) include tank used for storing ammonia (6), air compressor (7), air accumulator (8), centrifugal blower (9), air heater (10), vaporizer
(11), air accumulator (8) is 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, vaporizer (11) and denitration reaction component
(2) it is connected to, the ammonium hydroxide vaporization member (1) further includes absorption type dryer (33), absorption type dryer (33) one end and sky
Air compressor (7) connection, absorption type dryer (33) other end are connected to air accumulator (8).
3. flue gas nitrogen oxide processing system according to claim 1 or 2, it is characterised in that: the denitration reaction portion
Part (2) includes mixer (12) and reactor (13), and mixer (12) is connected to vaporizer (11), mixer (12) simultaneously with it is anti-
It answers device (13) to be connected to, the multiple catalyst of gap setting (5) is pressed in reactor (13), reactor (13) includes air inlet (14) and row
Port (15), reactor (13) press the multiple catalyst of gap setting (5) from air inlet (14) one end to exhaust outlet (15) one end.
4. flue gas nitrogen oxide processing system according to claim 1 or 2, it is characterised in that: the flue gas nitrogen oxidation
Object processing system further includes deashing component (16), and deashing component (16) setting is in denitration reaction component (2), deashing component (16)
Including compressed-air atomizer (17), compressed air reservoir (18), blowing control unit (19), each compressed-air atomizer (17) point
Not Tong Guo connecting line be connected to compressed air reservoir (18), setting can control compressed air and open on compressed air reservoir (18)
Stop and multiple compressed-air atomizers are arranged in the blowing control unit (19) of flow adjusting, the position close to each catalyst (5)
(17), the gas outlet close to multiple compressed-air atomizers (17) of each catalyst (5) is respectively aligned to the catalyst (5).
5. flue gas nitrogen oxide processing system according to claim 1, it is characterised in that: the vaporizer (11) includes
Atomizer (22) and gasifier (23), atomizer (22) one end are connected to air accumulator (8), atomizer (22) other end and gasifier
(23) it is connected to, air heater (10) is connected to gasifier (23), gasifier (23) mixing with denitration reaction component (2) simultaneously
Device (12) connection.
6. flue gas nitrogen oxide processing system according to claim 3, it is characterised in that: the denitration reaction component
It (2) further include part case (24), mixer (12) and reactor (13) are arranged in part case (24), reactor (13)
Air inlet (14) are arranged in upper end, and exhaust outlet (15) are arranged in reactor (13) lower end, position between catalyst (5) and air inlet (14)
It is arranged ash slot (25), ash slot (25) is connected to ash channel (26) one end, ash channel (26) other end and part case
(24) ash discharging hole (27) connection of lower end.
7. flue gas nitrogen oxide processing system according to claim 1 or 2, it is characterised in that: the catalyst (5) includes
First layer catalyst (28), second layer catalyst (29), third layer catalyst (30), the first layer catalyst (28) are located at
The upper position of reactor (2) inner space, second layer catalyst (29) are located at first layer catalyst (28) lower position, third
Layer catalyst (30) is located at second layer catalyst (29) lower position.
8. flue gas nitrogen oxide processing system according to claim 6, it is characterised in that: described ash channel (26) position
In ash slot (25) lower position, multiple compressed-air atomizers (17) are arranged in first layer catalyst (28) left side, and the second layer is urged
Agent (29) each side is respectively set one or more compressed-air atomizers (17), third layer catalyst (30) each side point
It She Zhi not one or more compressed-air atomizers (17).
9. flue gas nitrogen oxide processing system according to claim 6, it is characterised in that: on the ash channel (26)
It is arranged weight turning plate valve (31), the dust that ash slot (25) is transported to ash channel (26), which is configured to down to fall on weight, to be turned over
Structure on plate valve door (31), the dust whereabouts that ash slot (25) is transported to ash channel (26) are stacked into weight turning plate valve
(31) when the actual weight on is more than the setting weight numerical value of weight turning plate valve (31), weight turning plate valve (31) is arranged to
It is enough to open, enable the structure that ash discharging hole (27) discharge is fallen under the dust being deposited on weight turning plate valve (31).
10. flue gas nitrogen oxide processing system according to claim 1 or 2, it is characterised in that: the catalyst (5)
It further include preparing catalyst installation site (32), orientation is arranged under third catalyst (30) in preparing catalyst installation site (32)
It sets, the part case (24) in preparing catalyst installation site (32) lower position is arranged in the exhaust outlet (15) of reactor (13)
On.
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| CN201810551170.7A CN109731462A (en) | 2018-05-31 | 2018-05-31 | A flue gas nitrogen oxide treatment system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023053218A1 (en) | 2021-09-28 | 2023-04-06 | 三菱重工業株式会社 | Denitration device |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202893166U (en) * | 2012-04-28 | 2013-04-24 | 湖南大学 | Flue gas denitration device |
| CN103406006A (en) * | 2013-08-30 | 2013-11-27 | 安徽省元琛环保科技有限公司 | SCR (Selective Catalytic Reduction) denitration device for NOx control of rotary cement kiln |
| CN203862253U (en) * | 2014-06-10 | 2014-10-08 | 李灏呈 | SCR denitration catalyst regenerating and deashing device |
| CN104906952A (en) * | 2015-06-03 | 2015-09-16 | 北京凯盛建材工程有限公司 | SCR denitration system and method |
| CN105854537A (en) * | 2016-05-09 | 2016-08-17 | 清华大学 | Industrial furnace sulfur trioxide pre-removing and denitration device and method |
| CN105964142A (en) * | 2016-06-28 | 2016-09-28 | 江苏亿金环保科技有限公司 | Combined type flue gas denitration system |
| CN106621739A (en) * | 2016-12-27 | 2017-05-10 | 江苏科瑞工程设计有限公司 | Method for removing nitric oxides from regenerated flue gas of waste acid cracking device |
| CN108043210A (en) * | 2017-11-17 | 2018-05-18 | 山西省化工设计院 | A kind of desulfurization of coke oven flue gas and dedusting denitrification integral system |
| CN208512272U (en) * | 2018-05-31 | 2019-02-19 | 安徽海螺建材设计研究院有限责任公司 | Flue gas nitrogen oxide processing system |
-
2018
- 2018-05-31 CN CN201810551170.7A patent/CN109731462A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202893166U (en) * | 2012-04-28 | 2013-04-24 | 湖南大学 | Flue gas denitration device |
| CN103406006A (en) * | 2013-08-30 | 2013-11-27 | 安徽省元琛环保科技有限公司 | SCR (Selective Catalytic Reduction) denitration device for NOx control of rotary cement kiln |
| CN203862253U (en) * | 2014-06-10 | 2014-10-08 | 李灏呈 | SCR denitration catalyst regenerating and deashing device |
| CN104906952A (en) * | 2015-06-03 | 2015-09-16 | 北京凯盛建材工程有限公司 | SCR denitration system and method |
| CN105854537A (en) * | 2016-05-09 | 2016-08-17 | 清华大学 | Industrial furnace sulfur trioxide pre-removing and denitration device and method |
| CN105964142A (en) * | 2016-06-28 | 2016-09-28 | 江苏亿金环保科技有限公司 | Combined type flue gas denitration system |
| CN106621739A (en) * | 2016-12-27 | 2017-05-10 | 江苏科瑞工程设计有限公司 | Method for removing nitric oxides from regenerated flue gas of waste acid cracking device |
| CN108043210A (en) * | 2017-11-17 | 2018-05-18 | 山西省化工设计院 | A kind of desulfurization of coke oven flue gas and dedusting denitrification integral system |
| CN208512272U (en) * | 2018-05-31 | 2019-02-19 | 安徽海螺建材设计研究院有限责任公司 | Flue gas nitrogen oxide processing system |
Non-Patent Citations (1)
| Title |
|---|
| 全国勘察设计注册环保工程师专业管理委员会等, 中国环境科学出版社.北京 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023053218A1 (en) | 2021-09-28 | 2023-04-06 | 三菱重工業株式会社 | Denitration device |
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