CN104645828A - SCR denitration device and method applied to high-dust-content smoke from kiln tail of cement clinker production line - Google Patents
SCR denitration device and method applied to high-dust-content smoke from kiln tail of cement clinker production line Download PDFInfo
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Abstract
The invention discloses an SCR (selective catalytic reduction) denitration device and an SCR denitration method applied to high-dust-content smoke from a kiln tail of a cement clinker production line. The device comprises a cement kiln decomposing furnace, a preheater, an afterheat boiler, a raw mill, an electric dust remover and a kiln tail chimney which are connected in sequence along the smoke direction, and further comprises an SCR reactor, wherein the SCR reactor comprises a reactor shell; an inlet divergent section is arranged at the top of the reactor shell, and an ash bucket is arranged at the bottom of the reactor shell; an inlet flue of the SCR reactor is connected with the preheater and the inlet divergent section and is provided with a reducer sprayer; a plurality of catalyst layers are arranged in the reactor shell in sequence from top to bottom; a plurality of steam ash blowers correspond to the catalyst layers one to one and are arranged above the corresponding catalyst layers; an outlet flue of the SCR reactor is connected with the bottom of the reactor shell and an upstream flue or a downstream flue of the afterheat boiler and is additionally provided with a high-temperature fan. On the basis that a high-temperature dust remover is not arranged, the SCR denitration device can handle with the smoke characteristics of high NOx load fluctuation, temperature fluctuation and high dust content.
Description
Technical field
The invention belongs to industrial furnace flue gas nitrogen oxide Treatment process field, be specifically related to a kind of SCR denitration device and the method that are applied to cement clinker production line stove high-dust flue gas.
Background technology
NOx control technology for cement kiln dore furnace mainly contains three classes: low-NO_x combustion technology (LowNOx burner, LNB), selective non-catalytic reduction (Selective Non-CatalyticReduction, and SCR (Selective Catalytic Reduction, SCR) denitration technology SNCR).
Low-NO_x combustion technology comprises the means such as low-NOx combustor, fuel-staged combustion, Researched of Air Staging Combustion Burning Pulverized Coal, mainly set about from aspects such as the supply of control oxygen or reduction flue-gas temperatures, reduce the generation of thermal NO x, its denitration effect is subject to cement clinker calcining process restriction, denitration efficiency be it is generally acknowledged 15 ~ 30%, and stability is not good, generally as compounding technique, reduce initial NOx emission concentration, save reducing agent consumption.
SNCR denitration technology, is spray into containing amino reducing agent in the appropriate location of cement kiln dore furnace and exhaust pass, makes the NOx generated in flue gas be reduced to N
2.Key problem in technology is that spray site reaction zone temperature need remain on 850 ~ 1050 DEG C, and reducing agent can mix with flue gas, and denitration efficiency be it is generally acknowledged more than 60%.
SCR denitration technology refers in the reactor being mounted with catalyst, sprays into suitable amino reductive, and the NOx generated in flue gas in cement kiln is optionally reduced to N by nitrogen oxide in flue gas fast and efficiently
2, denitration efficiency be it is generally acknowledged more than 80%, ripe in thermal power plant's application, but cement industry application achievement is less.External cement kiln dore furnace SCR denitration technology only has 3 cases, domesticly still belongs to blank.Subject matter is catalyst problem and high dirt problem.
Such as, application number be 201310390521.8 Chinese invention patent application document disclose cement kiln flue gas high-temperature dust removal SCR denitration device, it is characterized in that: comprise the electric cleaner be connected with cement kiln preheaters, the output of electric cleaner is connected with blender by pipeline, blender is provided with compressed air inlet, reducing agent entrance and reducing agent spray gun, the output of blender is connected with SCR reactor by pipeline, be provided with catalyst in SCR reactor, SCR reactor output is provided with booster fan and the flue gas after purification is entered upstream device.The beneficial effect of this application: first high-temperature flue gas carries out depositing dust process by hot electrostatic precipitator, can effectively avoid flying dust to cause wearing and tearing, blocking and inactivation to SCR catalyst; Remove the CaO particle in cement kiln flue gas simultaneously, avoid CaO particle itself to cause blocking and and the SO of catalyst micropore
3the CaSO that reaction generates
4to the blocking that catalyst causes.
Hot precipitator is set, really effectively can solves high dirt in theory to the abrasion of catalyst, blocking and inactivation, but in Practical Project, there is the problems such as transformation difficulty is large, the pressure loss is large, power consumption is high.In addition, cement kiln dore furnace SCR reactor inlet cigarette temperature is about 320-350 DEG C, installs the temperature drop that High Temperature Pre dedusting causes additional, also can reduce the activity of catalyst.
Summary of the invention
The invention provides a kind of SCR denitration device and the method that are applied to cement clinker production line kiln tail high-dust flue gas, do not arranging on the basis of hot precipitator, the smoke transportation of high NOx load fluctuation, temperature fluctuation, high dust can be tackled, can accomplish that denitration efficiency reliable and stablely reaches more than 80%, the escaping of ammonia controls at 2.5mg/m
3below.
Be applied to a SCR denitration device for cement clinker production line kiln tail high-dust flue gas, comprise and move towards along flue gas the cement kiln dore furnace, preheater, waste heat boiler, raw mill, electric cleaner and the kiln tail chimney that connect successively; Also comprise SCR reactor, described SCR reactor comprises:
Reactor shell, this reactor shell top is with entrance divergent segment, and bottom is with ash bucket;
SCR reactor inlet flue, connects described preheater and entrance divergent segment, and this SCR reactor inlet flue arranges reducing agent injector;
Some catalyst layers, are successively set in described reactor shell from top to bottom;
Some soot blowers, are arranged at the top of corresponding catalyst layer with catalyst layer one_to_one corresponding;
SCR reactor outlet flue, the upstream flue of coupled reaction device housing bottom and waste heat boiler or the downstream flue of coupled reaction device housing bottom and waste heat boiler, high-temperature blower set up by this SCR reactor outlet flue.
The present invention is directed to high dirt environment, on the existing basis moving towards the cement kiln dore furnace preheater, waste heat boiler, raw mill, electric cleaner and the kiln tail chimney that connect successively along flue gas, SCR reactor is installed additional by transformation, High Temperature Pre deduster is not set, cement kiln end height dirt smoke evacuation environment can be successfully managed, and accomplish degree of depth denitration.With flue gas flow direction, flue gas converges flue appropriate point position from most higher level's (C1 level) cyclone cylinder outlet of cement kiln end preheater and draws high-temperature high dust flue gas, draw the place of connecing and electronic or pneumatic baffle door is set, flow through gas approach straight down, after completing Gas Parameters detection by flue gas inspection instrument, reducing agent is sprayed in appropriate point position, flue gas mixes with reducing agent, SCR reactor is entered through flue water conservancy diversion, SCR reactor inlet section is provided with gradually wealthy section, ensure that the flue gas flow field introducing SCR reactor is stablized, reactor straight section top is provided with rectifier, then successively by 3 ~ 6 layers of catalyst, after catalyst bed body completes catalytic denitration reaction, discharge from reactor lower part, discharge flue and set up high-temperature blower, in order to overcome the denitration reaction pressure loss, send flue gas back to existing flue system, successively via waste heat boiler, raw mill, deduster, kiln tail blower fan after funnel discharges.The SCR reactor that the present invention sets up is arranged between preheater and waste heat boiler by flue duct retrofit, and can ensure the temperature range that the reaction of SCR reaction denitration is suitable does not affect waste heat boiler thermal effect by rational INSULATION DESIGN again.
In the present invention, in SCR reactor front end, hot precipitator is not set, every layer of catalyst top is provided with steam sootblower and acoustic wave ash ejector combined unit, acoustic wave ash ejector breaks up big dust particle, steam sootblower is blown retaining in the ash bucket of bottom by soot blower to the exhaust gas dust on catalyst layer, and can tackle dust concentration scope is 20 ~ 100g/m
3.Catalyst 3 ~ 6 layers is adjustable, can tackle initial NOx emission concentration 300 ~ 1200mg/m
3, denitration rate can up to more than 90%.Apparatus of the present invention can be applied to high temperature denitration, and flue-gas temperature can reach 320-360 DEG C, can adapt to all cement kiln end preheater exiting flue gas row temperature.
Therefore, as preferably, described soot blower comprises acoustic wave ash ejector and steam sootblower, acoustic wave ash ejector and steam sootblower cooperation.
All catalyst layers are all configured with acoustic wave ash ejector and steam sootblower, the two synergy, and each soot blower independently arranges gauge tap, control by denitration control system is unified.Acoustic wave ash ejector and steam sootblower are arranged in 0.4-0.8m place, catalyst layer top.Further, be distributed on the both sides sidewall in reactor shell.Puffed rice dirt common in cement kiln flue gas is broken up by high pressure sound wave by acoustic wave ash ejector, and steam sootblower ensures the completeness of blowing ash, and dust is sent into air-flow and be beneficial to and discharge with flue gas.
High-temperature blower of the present invention, its impeller material height heatproof, wear-resisting, select guarantee 400 DEG C of indeformable, 100g/m
3dust content not worn out, configure variable-frequency motor in addition, reply is mounted with the pressure loss of the required reply of SCR reactor of different number of plies catalyst.This high-temperature blower can adopt commercially available prod.
Reducing agent is arranged on SCR reactor inlet flue, injection direction is parallel with flue gas flow direction, the reducing agent injector at SCR reactor inlet flue place adopts two-fluid spray ammonia barrier, can realize 150% flue interface coverage rate at 1m place, ammonia-spraying grid downstream, reducing agent adopts the ammoniacal liquor of 20-25wt%.
Reductant injection system of the present invention, is different from traditional SCR denitration system, and adopt two-fluid ammonia-spraying grid, liquid phase is that required reducing agent flows through passage, and gas phase strengthens atomizing effect and mixability further.
As preferably, described SCR reactor also comprises and is arranged in described reactor shell and is positioned at the rectifier in entrance divergent segment enlarging downstream.The entrance of SCR reactor arranges flaring mouth and stablizes flue gas/ammonia importing reactor, after entrance, rectifier is set, ensures that the NOx concentration field of whole SCR reactor inlet section, reductant concentration, temperature field, velocity field meet the requirement of general SCR reactor further.
As preferably, in described SCR reactor inlet flue, be provided with smoke deflector.Flue gas is imported in SCR reactor more smoothly.
As preferably, described SCR reactor inlet flue is provided with the first flue gas inspection instrument; Described SCR reactor outlet flue is provided with the second flue gas inspection instrument and ammonia detector.
First flue gas inspection instrument, the second flue gas inspection instrument, the escaping of ammonia detector signal all send into denitration control system, in order to metering and control ammonia spraying amount.
Denitration control system adopts classical control system, and the theory that denitration control system calculates needs ammonia amount, by the pneumatic control valve of reducing agent injector and mass flowmenter with the use of, determine actual ammoniacal liquor demand.
As preferably, be also provided with the storehouse pump be connected with described ash bucket.Smoothly the cigarette ash in ash bucket is delivered to subsequent treatment process by this storehouse pump.
As preferably, described catalyst layer is set to 3 ~ 6 layers; Most preferably, be set to 6 layers, load several 3 ~ 6 layers adjustable.
As preferably, the catalyst of described catalyst layer adopts cellular catalyst, and catalyst aperture is not less than 9mm, and wall thickness is not less than 1.5mm.Catalyst is GU Generic Unit, and sectional dimension is 150mmX150mm.
This cellular catalyst can adopt this area conventional catalyst, and the aperture of catalyst need meet above-mentioned requirements, to tackle high dirt environment.
SCR reactor of the present invention is arranged on the flue between kiln tail cyclone preheater and waste heat boiler, can directly flue duct retrofit be become tubular reactor or transform conventional scr reactor as; SCR reactor can successfully manage inlet NOx concentration fluctuation, and fluctuation range is at 250mg/m
3~ 1000mg/m
3, the low nitrogen in its upstream is transformed and the SNCR denitration system that puts into operation is normal or fault start and stop, does not affect the normal operation of SCR denitration system; SCR reactor can adopt ammoniacal liquor as reducing agent, then without the need to arranging liquefied ammonia system and supporting safety measure in addition, can save land used and operation and maintenance cost; SCR reactor is imported and exported flue and is arranged flue gas continuous on-line detection instrument (Continous Emmission MonitorSystem), and the flue gas inspection parameter of SCR reactor inlet end CEMS includes but not limited to: NOx concentration, flue gas flow, temperature, pressure, O
2content; SCR reactor outlet flue CEMS detected parameters includes but not limited to: NOx concentration, temperature, pressure, O
2; Reactor outlet also arranges the escaping of ammonia detector; SCR reactor catalyst bed arranges 6 layers, loads number 3-6 layer adjustable, tackles different load fluctuations; Rake steam sootblower is set above every layer of catalyst, and blow the grey frequency, blowing pressure, to blow grey tolerance adjustable, according to actual condition, timely ash discharge can be accomplished, can also accomplish energy-conservation; Every layer of catalyst arranges differential pressure transmitter, and signal delivers to control system, instruction catalyst blockage situation, and participates in blowing grey programme-control.
The flue that in the present invention, flue gas flows through, SCR reactor material main body select Q345 steel, and hot expansibility is good, have the local lined ceramics that the abrasion such as Wear-proof, smoke canal elbow reducing is serious, improve resistance to abrasion.
After the present invention directly can be installed at low nitrogen burning (LNB) that present cement plant has been configured, SNCR (SNCR) denitration, LNB-SNCR denitration, do not affect the use of the denitration facility built up, with the use of reducing reducing agent consumption.
The present invention uses the ammoniacal liquor of 20 ~ 25wt% as reducing agent, better can adapt to the existing situation in cement plant, and without the need to increasing liquefied ammonia system, flow process is simple, floor space is little, operation and maintenance cost is low.
Present invention also offers a kind of method utilizing described device to carry out cement kiln dore furnace denitrating flue gas, cement kiln dore furnace kiln exit gas is successively through preheater, waste heat boiler, got rid of by kiln tail chimney after raw mill and electric cleaner process, described kiln exit gas after preheater preheats process through by SCR reactor inlet flue, entrance divergent segment is introduced in SCR reactor, reducing agent is sprayed in SCR reactor inlet flue, each catalyst layer is flowed through successively after flue gas mixes with reducing agent, upstream flue or the downstream flue of preboiler is finally sent into by SCR reactor outlet flue and high-temperature blower, while flue gas flows through catalyst layer, the dust in flue gas blows in ash bucket by soot blower.
Processing method of the present invention is on the basis that existing kiln exit gas is discharged by kiln tail chimney successively after preheater, waste heat boiler, raw mill and deduster process, flue gas after preheater is got rid of is sent in the SCR reactor that the present invention installs additional and is carried out catalytic reaction, to tackle the unmanageable problem of cement kiln dore furnace kiln exit gas height dust.
Compared with prior art, the present invention has following technique effect:
(1) technology selected by, by improving Optimization of material selection design, Selection of Catalyst optimal design, SCR structure of reactor form optimal design, soot blower optimal design, solve high dirt to the abrasion of catalyst, corrosion and poisoning, and the system abrasion perforation caused;
(2) flue contacted with high-temperature high dust gas and SCR reactor body material selection Q345 steel, hot expansibility is good, has the local lined ceramics that the abrasion such as Wear-proof, smoke canal elbow reducing is serious, improves resistance to abrasion;
(3) 80-100g/m is tackled
3high dirt environment, the large wall thickness design in the large aperture of catalyst aperture and surface velocity, the blocking that low flow velocity can be avoided to cause and abrasion that is poisoning, that high flow rate can be avoided to cause again.
(4) SCR reactor lower end arranges gradually wealthy section and ash bucket, is discharged by dust settling by reducing flue gas flow rate by ash bucket;
(5) SCR reactor draught fan impeller material has high erosion resistance, improves the stability of a system;
(6) can, as existing low nitrogen or the extended technology of SNCR denitration technology, accomplish save reducing agent, degree of depth denitration and reduce emission intensity.
Accompanying drawing explanation
Fig. 1 is the structural representation of one embodiment of the present invention.
Fig. 2 is the structural representation of another embodiment of the present invention.
Shown in figure, Reference numeral is as follows:
1-cement kiln dore furnace 2-kiln tail flue 3-preheater
4-flue gas inspection instrument 5-conditioning Tower 6-waste heat boiler (CEMS-1)
7-first flue gas inspection instrument 8-entrance divergent segment 9-soot blower
10-booster fan 11-second flue gas inspection instrument 12-ammonia detector
13-catalyst layer 14-storehouse pump 15-electric cleaner
16-high-temperature blower 17-raw material bucket 18-kiln tail chimney
19-SCR reactor inlet cigarette 20-reactor shell 21-SCR reactor outlet flue road.
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is further illustrated, but not as the foundation limited the present invention.
As depicted in figs. 1 and 2, a kind of SCR denitration device being applied to clinker kiln exit gas, the kiln tail flue 2 of cement kiln dore furnace 1 is connected to preheater 3, kiln tail flue is provided with ammonia water spray device, ammoniacal liquor is sprayed in kiln tail flue, preheater adopts Pyatyi preheater, kiln tail flue is connected to C5 (bottom) preheater of Pyatyi preheater, conditioning Tower 5 and waste heat boiler 6 are set up in parallel, both upstream flues are all connected with C1 (most top layer) preheater of Pyatyi preheater, raw mill 17 is connected to after both downstream flue merging, raw mill downstream arranges electric cleaner 15, electric cleaner downstream arranges kiln tail chimney 18, flue near C1 (most top layer) preheater place is provided with flue gas monitoring instrument (CEMS-1) 4, above-mentioned accessory and connected mode all adopt this area conventional means.
Device of the present invention focuses on the SCR reactor set up, this SCR reactor is set up on the bypass flue of waste heat boiler, SCR reactor comprises reactor shell 20, reactor shell 20 top is with entrance divergent segment 8, the enlarging of entrance divergent segment 8 is connected with reactor shell 20, reducing place of entrance divergent segment connects SCR reactor inlet flue 19, SCR reactor inlet flue 19 is connected to the C1 preheater of Pyatyi preheater 3, in SCR reactor inlet flue 19, smoke deflector is set, SCR reactor inlet flue 19 also arranges reducing agent injector, this reducing agent injector injector adopts two-fluid spray ammonia barrier, the bottom of reactor shell arranges ash bucket, ash bucket connects storehouse pump 14.
The enlarging place downstream of entrance divergent segment 8 arranges rectifier, 3 ~ 6 layers of catalyst layer 13 are set gradually from top to bottom below rectifier, the top correspondence of every layer of catalyst layer arranges a soot blower 9, soot blower comprises acoustic wave ash ejector and steam sootblower, the two conbined usage, all be arranged on 0.4 ~ 0.8m place above corresponding catalyst layer, steam sootblower adopts rake steam sootblower, steam sootblower external compressed air.
The bottom of reactor shell connects SCR reactor outlet flue 21, this exhaust pass is arranged a booster fan 10, and at added downstream high-temperature blower 16 of booster fan, this high-temperature blower adopts commercially available prod, the upstream flue (as Fig. 1) of downstream flue access waste heat boiler 6 of high-temperature blower or the downstream flue (as Fig. 2) of access waste heat boiler 6.
SCR reactor inlet flue 19 is arranged and the first flue gas inspection instrument 7, SCR reactor outlet flue 21 arranges the second flue gas inspection instrument 11 and ammonia detector 12, first flue gas inspection instrument and the second flue gas inspection instrument is flue gas continuous on-line detection instrument.
All flue gas inspection instrument are all connected to denitration control system with peace detector and reducing agent injector, and denitration control system and control method adopt the control technology of this area maturation.
Cement kiln dore furnace kiln exit gas is got rid of by kiln tail chimney 18 successively after the process of preheater 3, conditioning Tower 5, waste heat boiler 6, raw mill 17 and electric cleaner 15, kiln exit gas warp after preheater preheats process is introduced in SCR reactor by SCR reactor inlet flue 19, entrance divergent segment 8, reducing agent is sprayed in SCR reactor inlet flue 19, flow through each catalyst layer 13 after flue gas mixes with reducing agent successively, finally sent into upstream flue or the downstream flue of preboiler by SCR reactor outlet flue 21 and high-temperature blower 16; While flue gas flows through catalyst layer, the dust in flue gas blows in ash bucket by soot blower 9.
Embodiment 1
This embodiment is according to device and technique as shown in Figure 1.Cement kiln dore furnace 10000Nm
3/ h bypass flue gas SCR denitration experimental rig, arranges bypass in waste heat boiler front and back end, draws actual flue gas, flue-gas temperature 350 DEG C ± 20 DEG C, dustiness 30-100g/m
3, (there has been configuration SNCR denitration device SCR denitration reactor upstream to NOx initial concentration 280-1200mg/m3, if upstream SNCR denitration device does not put into operation, initial concentration is up to 700-1200mg/m
3, after upstream SNCR denitration device puts into operation, the minimum NOx emission concentration that can control is at 200mg/m
3, generally control at 320mg/m according to standard
3below, therefore, inlet NOx concentration is adjustable on a large scale.
Refer to accompanying drawing 1, the bypass flue that kiln tail waste heat boiler front and back end is arranged configures SCR denitration reactor, bypass flue gas experiences flue deflector, SCR reactor inlet divergent segment, rectifier, the first catalyst layer, the second catalyst layer, the 3rd catalyst layer, the 4th catalyst layer, the 4th catalyst layer, the 6th catalyst layer, SCR reactor outlet flue, air-introduced machine successively along flue gas direction, drain into waste heat boiler downstream flue, be incorporated to main body flue gas.
Wherein every layer of catalyst top is provided with steam sootblower, purge pressure 0.8MPa, reducing agent is arranged on SCR reactor inlet flue, injection direction is parallel with flue gas flow direction, reducing agent adopts the ammoniacal liquor of 20-25wt%, SCR reactor lower part is provided with ash bucket, SCR reactor inlet flue is provided with the first flue gas on-line detector, monitoring index has NOx, flue gas flow Q, flue-gas temperature T, flue gas oxygen content, SCR reactor outlet flue is provided with the 2nd CEMS, and monitoring index has NOx concentration, flue gas flow Q, flue-gas temperature T, flue gas oxygen content, NH
3concentration.
Under the condition that SNCR denitration device puts into operation, on a CEMS, NOx concentration is 280-320mg/m
3, ammoniacal liquor consumption is when 5l/h, and the second flue gas inspection instrument NOx concentration is 140-160mg/m
3, denitration efficiency is about 50%; When ammoniacal liquor consumption is 10l/h, on the 2nd CEMS, NOx concentration is 50-75mg/m
3, denitration efficiency is about 80%; When ammoniacal liquor consumption is 15l/h, on the 2nd CEMS, NOx concentration is 15-35mg/m
3, denitration rate can be high by 95%, the equal < 3mg/m of emission intensity concentration
3;
Under the condition that SNCR denitration device is stopped transport, on a CEMS, NOx concentration is 750-1200mg/m
3, ammoniacal liquor consumption is when 10l/h, and the second flue gas inspection instrument NOx concentration is 320-500mg/m
3, denitration efficiency is about 50%; When ammoniacal liquor consumption is 15l/h, on the 2nd CEMS, NOx concentration is 140-160mg/m
3, denitration efficiency is about 80%; When ammoniacal liquor consumption is 20l/h, on the 2nd CEMS, NOx concentration is 35-50mg/m
3, denitration rate about 95%, the equal < 3mg/m of emission intensity concentration
3; .
Embodiment 2
This embodiment is according to device and technique as shown in Figure 2.The cement kiln dore furnace SCR denitration engineering of daily output 2500t grog, the denitration of the full flue gas degree of depth, exhaust gas volumn 295000m
3/ h, flue-gas temperature 350 DEG C ± 20 DEG C, dustiness 30-100g/m
3, NOx initial concentration 280-1200mg/m
3(there has been configuration SNCR denitration device SCR denitration reactor upstream, if upstream SNCR denitration device does not put into operation, initial concentration is up to 700-1200mg/m
3, after upstream SNCR denitration device puts into operation, the minimum NOx emission concentration that can control is at 200mg/m
3, generally control at 320mg/m according to standard
3below, therefore, inlet NOx concentration is adjustable on a large scale.
Refer to accompanying drawing 2, SCR denitration reactor is set up in waste heat boiler front end, after denitration, flue gas drains into preboiler, flue gas experiences flue deflector, SCR reactor inlet divergent segment, rectifier, the first catalyst layer, the second catalyst layer, the 3rd catalyst layer, the 4th catalyst layer, the 5th catalyst layer, the 6th catalyst layer, SCR reactor outlet flue, air-introduced machine successively along flue gas direction, drain into waste heat boiler upstream trip flue, successively after waste heat boiler, high-temperature blower, raw mill, deduster, drain into kiln tail chimney by kiln tail blower fan.
Wherein every layer of catalyst top is provided with steam sootblower, reducing agent is arranged on SCR reactor inlet flue, injection direction is parallel with flue gas flow direction, 150% flue interface coverage rate can be realized at 1m place, ammonia-spraying grid downstream, reducing agent adopts the ammoniacal liquor of 20-25wt%, SCR reactor lower part is provided with ash bucket, SCR reactor inlet flue is provided with the first flue gas on-line detector, monitoring index has NOx, flue gas flow Q, flue-gas temperature T, flue gas oxygen content, SCR reactor outlet flue is provided with the 2nd CEMS, monitoring index has index to have NOx concentration, flue gas flow Q, flue-gas temperature T, flue gas oxygen content, NH
3concentration.
Under the condition that SNCR denitration device puts into operation, on a CEMS, NOx concentration is 280-320mg/m
3, ammoniacal liquor consumption is when 100l/h, and the second flue gas inspection instrument NOx concentration is 130-165mg/m
3, denitration efficiency is about 50%; When ammoniacal liquor consumption is 150l/h, on the 2nd CEMS, NOx concentration is 50-80mg/m
3, denitration efficiency is about 80; When ammoniacal liquor consumption is 200l/h, on the 2nd CEMS, NOx concentration is 15-35mg/m
3, denitration rate 95%;
Under the condition that SNCR denitration device is stopped transport, on a CEMS, NOx concentration is 750-800mg/m
3, ammoniacal liquor consumption is when 300l/h, and the second flue gas inspection instrument NOx concentration is 140-160mg/m
3, denitration efficiency is about 50%; When ammoniacal liquor consumption is 450l/h, on the 2nd CEMS, NOx concentration is 140-160mg/m
3, denitration efficiency is about 80%; When ammoniacal liquor consumption is 600l/h, on the 2nd CEMS, NOx concentration is 50mg/m
3, denitration rate 95%, the equal < 3mg/m of emission intensity concentration
3.
Claims (10)
1. be applied to a SCR denitration device for cement clinker production line kiln tail high-dust flue gas, comprise and move towards along flue gas the cement kiln dore furnace, preheater, waste heat boiler, raw mill, electric cleaner and the kiln tail chimney that connect successively; It is characterized in that, also comprise SCR reactor, described SCR reactor comprises:
Reactor shell, this reactor shell top is with entrance divergent segment, and bottom is with ash bucket;
SCR reactor inlet flue, connects described preheater and entrance divergent segment, and this SCR reactor inlet flue arranges reducing agent injector;
Some catalyst layers, are successively set in described reactor shell from top to bottom;
Some soot blowers, are arranged at the top of corresponding catalyst layer with catalyst layer one_to_one corresponding;
SCR reactor outlet flue, the upstream flue of coupled reaction device housing bottom and waste heat boiler or the downstream flue of coupled reaction device housing bottom and waste heat boiler, high-temperature blower set up by this SCR reactor outlet flue.
2. be applied to the SCR denitration device of cement clinker production line kiln tail high-dust flue gas according to claim 1, it is characterized in that, described SCR reactor also comprises and is arranged in described reactor shell and is positioned at the rectifier in entrance divergent segment enlarging downstream.
3. be applied to the SCR denitration device of cement clinker production line kiln tail high-dust flue gas according to claim 1, it is characterized in that, in described SCR reactor inlet flue, be provided with smoke deflector.
4. be applied to the SCR denitration device of cement clinker production line kiln tail high-dust flue gas according to claim 1, it is characterized in that, described SCR reactor inlet flue is provided with the first flue gas inspection instrument.
5. be applied to the SCR denitration device of cement clinker production line kiln tail high-dust flue gas according to claim 1, it is characterized in that, described SCR reactor outlet flue is provided with the second flue gas inspection instrument and ammonia detector.
6. be applied to the SCR denitration device of cement clinker production line kiln tail high-dust flue gas according to claim 1, it is characterized in that, be also provided with the storehouse pump be connected with described ash bucket.
7. be applied to the SCR denitration device of cement clinker production line kiln tail high-dust flue gas according to claim 1, it is characterized in that, described catalyst layer is set to 3 ~ 6 layers.
8. be applied to the SCR denitration device of cement clinker production line kiln tail high-dust flue gas according to claim 1, it is characterized in that, described soot blower comprises acoustic wave ash ejector and steam sootblower, acoustic wave ash ejector and steam sootblower cooperation.
9. be applied to the SCR denitration device of cement clinker production line kiln tail high-dust flue gas according to claim 1, it is characterized in that, the catalyst of described catalyst layer adopts cellular catalyst, and catalyst aperture is not less than 9mm, and wall thickness is not less than 1.5mm.
10. utilize the arbitrary described device of claim 1 ~ 9 to carry out a method for cement kiln dore furnace denitrating flue gas, cement kiln dore furnace kiln exit gas is got rid of by kiln tail chimney successively after preheater, waste heat boiler, raw mill and electric cleaner process,
It is characterized in that,
Described kiln exit gas warp after preheater preheats process is introduced in SCR reactor by SCR reactor inlet flue, entrance divergent segment, reducing agent is sprayed in SCR reactor inlet flue, flow through each catalyst layer successively after flue gas mixes with reducing agent, finally sent into upstream flue or the downstream flue of preboiler by SCR reactor outlet flue and high-temperature blower; While flue gas flows through catalyst layer, the dust in flue gas blows in ash bucket by soot blower.
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