CN106595294A - Special type catalytic reduction method composite denitration system - Google Patents
Special type catalytic reduction method composite denitration system Download PDFInfo
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- CN106595294A CN106595294A CN201610889311.7A CN201610889311A CN106595294A CN 106595294 A CN106595294 A CN 106595294A CN 201610889311 A CN201610889311 A CN 201610889311A CN 106595294 A CN106595294 A CN 106595294A
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
- F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
- F27B7/34—Arrangements of heating devices
-
- 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
-
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D1/00—Burners for combustion of pulverulent fuel
- F23D1/02—Vortex burners, e.g. for cyclone-type combustion apparatus
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
The invention relates to a special type catalytic reduction method composite denitration system. The system comprises a rotary kiln, a kiln tail smoke chamber arranged at the tail of the rotary kiln and a decomposing furnace, and further comprises a smoke chamber flue extending pipe, a low-nitrogen burner, a kiln tail steam catalytic unit, a tertiary air inlet and a C4 discharging pipe; the C4 discharging pipe comprises two symmetrically-arranged discharging pipe bodies, two dividing valves and two discharging branch pipes, and the two discharging branch pipes are composed of two upper branch pipe bodies and two lower branch pipe bodies; and the kiln tail steam catalytic unit comprises three steam spraying nozzles, an annular pipe, a steam catalyst tank, a flowmeter, a control valve, a steam source and a catalyst. On the premise that nitrogen oxide emission is unchanged, the using amount of a reducing agent, namely ammonium hydroxide of the SNCR denitration system can be saved by 50% to 100%, and ammonia escape is reduced by 5 milligrams per cubic meter to 10 milligrams per cubic meter. Pollution of nitrogen oxide emission to the atmosphere is effectively avoided, no new pollution source is generated, and the very good application and popularization value can be achieved.
Description
Technical field
The invention belongs to environmental technology field, more particularly to a kind of special type catalysis suitable for dry-process cement clinker production line
Reducing process composite denitration system.
Background technology
According to the data that Chinese cement net and Chinese cement association issue：The cement annual capacity of China in 2012 is up to 2,500,000,000
Ton, existing novel dry-method cement clinker production line 2000 are a plurality of, and the nitrogen oxide emission in cement production process accounts for national nitrogen
The 15%～20% of emissions of oxides total amount, cement manufacturers nitrogen oxides and sulfide emission administer extremely urgent,
Pollutant are reduced using fractional combustion, SNCR mode denitrations, the ammonia process of desulfurization and calcium method desulphation mode more than Present Cement manufacturing enterprise
Discharge capacity, but the escaping of ammonia that above-mentioned technique is caused causes secondary pollution again to air, therefore improve and improve above-mentioned technique, cut
The real the escaping of ammonia for reducing discharged nitrous oxides and producing in reducing nitrogen oxides governance process is inexorable trend.And it is existing
SNCR denitration technique, reducing agent ammonia（20% content）Consumption substantially in 3-5 kg/t grogs, the escaping of ammonia in 5-12PPm or so,
Ton grog denitration cost 2-5 units/t, cause cement production enterprise to increase by ten thousand yuan of production cost 300-800 every year.
The content of the invention
In order to solve the above problems, it is an object of the invention to provide a kind of simple structure, improves SNCR denitration efficiency, reduces
The discharge of NOx, reduces ammonia volume and reduces the extraordinary catalytic reduction method composite denitration system of amount of ammonia slip.
The technical scheme is that：Extraordinary catalytic reduction method composite denitration system, the system include rotary kiln, kiln tail cigarette
Room, smoke-box flue and dore furnace, the system also include smoke-box flue extension tube, low NO, the vapor catalyzed device of kiln tail, three
Secondary wind air inlet and C4 tremie pipes；
The C4 tremie pipes include 2 symmetrically arranged tremie pipes, 2 material distributing valves and 2 blanking arms, 2 blankings
Pipe is made up of 2 upper arms and 2 lower branch lines,
The vapor catalyzed device of the kiln tail include 3 steam jets, circulating line, air inlet pipe, vapor catalyzed dose of tank, effusion meter,
Control valve, vapour source and catalyst；
The kiln tail smoke-box is arranged on the afterbody of rotary kiln, and the kiln tail smoke-box is provided with the smoke-box flue, the smoke-box flue
Extension tube is arranged on the smoke-box flue, and is connected with the dore furnace, and the lower furnace body lower end of the dore furnace is arranged with
One seasoning spreading box, 2 symmetrically arranged tremie pipe one end are connected with the discharging opening of self-discharging cyclone cylinder, the other end respectively with 2
The charging aperture connection of one seasoning spreading box, the tertiary air air inlet are arranged on and the dore furnace in the first seasoning spreading box same level
On body of heater, 2 described upper arm one end are connected with the middle part of 2 tremie pipes by material distributing valve respectively, 2 upper arms
The other end be connected with one end of 2 lower branch lines respectively, the other end of 2 lower branch lines is respectively equipped with the second spreading
Box, 2 second seasoning spreading boxes are symmetricly set on the smoke-box flue, are arranged with the smoke-box flue of the second seasoning spreading box
Plane in be also set in distance and have 3 low NOs and 3 steam jets, 3 low NOs and 3 steamings
The centrage of the downward-sloping setting of vapour nozzle, the low NO and the steam jet and the central shaft of the dore furnace
Angle between line is a, and a=15 °, 3 steam jets are connected with the circulating line arranged on the outside of smoke-box flue, the ring pipe
Road is connected with vapor catalyzed dose of tank by air inlet pipe, and the vapor catalyzed dose of tank passes through effusion meter and control valve and the vapour source
Connection；The low NO is connected with a point coal device by pipeline.
Further, the system also includes the vapor catalyzed device of kiln hood, the vapor catalyzed device steam jet of the kiln hood, air inlet
Pipe, vapor catalyzed dose of tank, effusion meter, control valve, vapour source and catalyst.
Further, the structure of first seasoning spreading box and the second seasoning spreading box is identical, and structure is：Splicing plate, spreading plate and with
Charging aperture that C4 tremie pipes are connected and with decompose the discharging opening that furnace body is connected, the splicing plate and spreading plate are end to end,
Overall is in sector, and, in 30 degree of overturning angles settings, the inner surface of the splicing plate is stepped for the splicing plate, and ladder is no less than
5 grades, the spreading plate is equipped with compressed air spout, the splicing on each section ladder of the splicing plate in horizontally disposed
Plate bottom is provided with discloses material hole, and the length of the spreading plate is not less than 30 centimetres.
Further, the low NO, including housing, jet pipe, swirl vanes and air inlet；The housing be provided with into
Air port, the jet pipe are arranged on the enclosure interior, and the end of the jet pipe is connected with pipeline, and the swirl vanes socket is in place
Between jet pipe front end and air inlet on the jet pipe, the blade of the swirl vanes is twisted blade, and blade is from air intake
Angle to outlet air end distortion is 90 °, is 0 in air intake blade face and axial angle, i.e., parallel with x-axis, then waits radian
Uniform gradually transition, when transitting to outlet air end, blade face and x-axis angle are 45 °.
Further, a diameter of 20-30cm of the nozzle of the low NO.
Further, the cross section of the smoke-box flue and the smoke-box flue extension tube is circle, and the smoke-box flue
The length of extension tube is not less than 1m.
Further, the flow of the vapor in the vapor catalyzed device of the kiln hood is 80-100kg/h, the vapor
Originate as waste heat boiler saturated vapor, temperature is 200-300 DEG C.
Further, the mass percent of each component of the catalyst：Nickel 25-30%, titanium 15-25%, chromium 5-15%, silicon
15-25%, calcium 10%, remaining as inevitable impurity.
The present invention principle be：The system will set up the prolongation of smoke-box flue between dore furnace hypocentrum and smoke-box flue
Pipe, and circular body is revised as in the cross section of smoke-box flue and smoke-box flue extension tube, the time of coal dust firing is extended, is made
Low NO position moves down, and after coal dust sprays into dore furnace, can be burnt, thus on smoke-box in less space
The conical section of the following dore furnace of Fang Yuzhi tertiary air air inlets forms an oxygen-poor reduction combustion zone, while the waste heat for introducing is sent out
Electric saturated vapor is vaporized and the activated hydrogen with reduction characteristic at high operating temperatures, with the penetrating oxygen-poor reduction combustion zone
Mix with coal dust, with reference to the tertiary air containing sufficient oxygen of dore furnace is entered from three air inlets in dore furnace lower furnace body
Fully burnt with coal dust and carbon monoxide middle and upper part；Make coal dust that going back similar to water gas is generated under high temperature environment
Former agent, and the row of NOx is reduced in catalytic action, the nitrogen that the NOx formed in rotary kiln is reduced to clean using this reducing agent
High-volume, while suppressing nitrogen oxides in dore furnace to quickly generate；Suppress the generation of fuel NO and reach denitration
Purpose.
Kiln tail smoke-box ascending air contains the oxygen of 3.5%-4.5%, and the coal dust of penetrating can burn in the region, and burning is caused
Raise the regional temperature, skinning is formed with increase trend, in order to solve the problems, such as that skinning increases, while by level Four blanking
Pipe branch is attached to above the low NO of smoke-box flue be that the temperature for reducing the region using the raw material for branching away is maintained
In 1150 degrees centigrades, it is to avoid refractory material is caused damage, the generation of skinning is prevented and is reduced；The environment temperature for maintaining simultaneously
Degree is adapted to reducing agent and the nitrogen oxides that system is produced is reduced to free of contamination nitrogen, reduces ammonia usage amount and the escaping of ammonia, ammonia
Water consumption can reduce 50-100% on year-on-year basis.It is fairly obvious to the energy-saving and NOx abatement effect of grog production process.
Present invention has the advantages that：Due to adopting above-mentioned technical proposal, the present invention produce class by above-mentioned technological transformation
The reducing agent of water gas is similar to, the thermal NO x that can be produced effectively in reduction kiln suppresses the generation of fuel type NOx, from source
The upper generation for effectively reducing NOx.Non-secondary pollution, no pollutant or by-product are generated.Clinker production line is run and grog
Yield and quality has no adverse effects.SNCR is run without negative effect, reduce ammonia or carbamide consumption, reduce reducing agent operating cost.
Operational factor is optimised, and lifts grog yield and quality, and energy conservation and consumption reduction effects are notable.Former SNCR denitration system is protected without negative effect
Under card clinker production line yield and quality is without negative effect precondition, SNCR denitration ammonia volume reduces by more than 50%, implements effective
Reduce NOXDischarge capacity（5000t/d cement producing lines can reduce NO every yearX1600 tons or so of discharge）, improve air ambient matter
Amount；Change impression of the common people to conventional cement industry；Enhance the supporting role that cement industry develops to national recycling economy；
The control ability to pollutant diffusion is improve, the show-how pattern of sustainable development is set up in cement production enterprise, to carrying
High technology in cement industry level, environmental protection and energy-saving and emission-reduction are significant；
Above-mentioned technology energy-saving effect after novel dry-method cement clinker production line application is very notable：It is constant in discharged nitrous oxides
On the premise of can save SNCR denitration system reducing agent ammonia volume 50%-100%, reduce per cube of the escaping of ammonia 5-10 milligrams
Rice.Efficiently solve the pollution that discharged nitrous oxides are caused to air, and do not have new polluter to produce, with pushing away well
Wide using value.So that one is produced daily 5000 tons of clinker production lines as an example, every year may be used in the constant situation of discharged nitrous oxides concentration
Think that enterprise saves ten thousand yuan of ammonia expense 200-450.
Description of the drawings
Fig. 1 is the structural representation of the extraordinary catalytic reduction method composite denitration system of the present invention.
Fig. 2 is enlarged diagram at A in Fig. 1.
Fig. 3 is the smoke-box flue schematic top plan view in present system.
Structural representations of the Fig. 4 for the seasoning spreading box in present system.
Schematic top plan views of the Fig. 5 for the seasoning spreading box in present system.
Fig. 6 is the vapor catalyzed apparatus structure schematic diagram of kiln hood in present system.
Structural representations of the Fig. 7 for the low NO in present system.
Structural representations of the Fig. 8 for the swirl vanes of the low NO in present system.
Specific embodiment
With reference to the accompanying drawings and detailed description technical scheme is described further.
As shown in figs 1 to 6, present invention special type catalytic reduction method composite denitration system, the system include rotary kiln, kiln tail
Smoke-box, smoke-box flue and dore furnace, the system also include smoke-box flue extension tube, low NO, the vapor catalyzed device of kiln tail,
Tertiary air air inlet and C4 tremie pipes；
The C4 tremie pipes include 2 symmetrically arranged tremie pipes, 2 material distributing valves and 2 blanking arms, 2 blankings
Pipe is made up of 2 upper arms and 2 lower branch lines,
The vapor catalyzed device of the kiln tail include 3 steam jets, circulating line, air inlet pipe, vapor catalyzed dose of tank, effusion meter,
Control valve, vapour source and catalyst；
The kiln tail smoke-box is arranged on the afterbody of rotary kiln, and the kiln tail smoke-box is provided with the smoke-box flue, the smoke-box flue
Extension tube is arranged on the smoke-box flue, and is connected with the dore furnace, and the lower furnace body lower end of the dore furnace is arranged with
One seasoning spreading box, 2 symmetrically arranged tremie pipe one end are connected with the discharging opening of self-discharging cyclone cylinder, the other end respectively with 2
The charging aperture connection of one seasoning spreading box, the tertiary air air inlet are arranged on and the dore furnace in the first seasoning spreading box same level
On body of heater, 2 described upper arm one end are connected with the middle part of 2 tremie pipes by material distributing valve respectively, 2 upper arms
The other end be connected with one end of 2 lower branch lines respectively, the other end of 2 lower branch lines is respectively equipped with the second spreading
Box, 2 second seasoning spreading boxes are symmetricly set on the smoke-box flue, are arranged with the smoke-box flue of the second seasoning spreading box
Plane in be also set in distance and have 3 low NOs and 3 steam jets, 3 low NOs and 3 steamings
The centrage of the downward-sloping setting of vapour nozzle, the low NO and the steam jet and the central shaft of the dore furnace
Angle between line is a, and a=15 °, 3 steam jets are connected with the circulating line arranged on the outside of smoke-box flue, the ring pipe
Road is connected with vapor catalyzed dose of tank by air inlet pipe, and the vapor catalyzed dose of tank passes through effusion meter and control valve and the vapour source
Connection；The low NO is connected with a point coal device by pipeline.
The system also includes the vapor catalyzed device of kiln hood, the vapor catalyzed device steam jet of the kiln hood, air inlet pipe, steam
Catalyst tank, effusion meter, control valve, vapour source and catalyst.
The structure of first seasoning spreading box and the second seasoning spreading box is identical, and structure is：Splicing plate, spreading plate and with C4 tremie pipes
The charging aperture that is connected and with decompose the discharging opening that furnace body be connected, the splicing plate and spreading plate are end to end, overall in fanning
Shape, the splicing plate are arranged in 30 degree of overturning angles, and the inner surface of the splicing plate is stepped, and ladder is no less than 5 grades, described
Spreading plate is equipped with compressed air spout in horizontally disposed on each section ladder of the splicing plate, the splicing plate bottom sets
Material hole is disclosed, the length of the spreading plate is not less than 30 centimetres.
The low NO, including housing, jet pipe, swirl vanes and air inlet；The housing is provided with air inlet, institute
State jet pipe and be arranged on the enclosure interior, the end of the jet pipe is connected with pipeline, and the swirl vanes are socketed in positioned at jet pipe
Between front end and air inlet on the jet pipe, the blade of the swirl vanes is twisted blade, and blade is from air intake to air-out
The angle of end distortion is 90 °, is 0 with axial angle in air intake blade face, i.e., parallel with x-axis, then wait radian uniformly by
Gradual transition, when transitting to outlet air end, blade face and x-axis angle are 45 °.
A diameter of 20-30cm of the nozzle of the low NO.
The cross section of the smoke-box flue and the smoke-box flue extension tube is circle, and the smoke-box flue extension tube
Length is not less than 1m.
The flow of the vapor in the vapor catalyzed device of the kiln hood is 80-100kg/h, and the source of the vapor is
Waste heat boiler saturated vapor, temperature are 200-300 DEG C.
The mass percent of each component of the catalyst：Nickel 25-30%, titanium 15-25%, chromium 5-15%, silicon 15-25%,
Calcium 10%, remaining as inevitable impurity.
Claims (9)
1. a kind of extraordinary catalytic reduction method composite denitration system, the system include rotary kiln, are arranged on the kiln tail of rotary kiln afterbody
Smoke-box and dore furnace（3）, it is characterised in that the system also includes smoke-box flue extension tube（11）, low NO（14）、
The vapor catalyzed device of kiln tail（9）, tertiary air air inlet（6）With C4 tremie pipes（5）；
The C4 tremie pipes（5）Including 2 symmetrically arranged tremie pipes（5-1）, 2 material distributing valves（5-2）With 2 blanking arms
（5-3）, 2 blanking arms are by 2 upper arms（5-3）With 2 lower branch lines（5-4）Composition,
The vapor catalyzed device of the kiln tail（9）Including 3 steam jets（9-1）, circulating line（9-2）, vapor catalyzed dose of tank（9-
3）, effusion meter（9-4）, control valve（9-5）, vapour source（9-6）And catalyst（13）；
Wherein, the smoke-box flue extension tube（11）One end and dore furnace（3）Hypocentrum end connection, kiln described in the other end
The smoke-box flue of tail smoke-box（4）Connection, the dore furnace（3）Lower furnace body（16）The side wall positioned at middle part on be symmetrically arranged with
First seasoning spreading box（8）, 2 symmetrically arranged tremie pipes（5-1）One end and self-discharging cyclone cylinder（7）Discharging opening connection, it is another
End respectively with 2 the first seasoning spreading boxes（8）Charging aperture connection, the tertiary air air inlet（6）It is arranged on and the first seasoning spreading box（8）
Dore furnace in same level（3）Body of heater on, 2 upper arms（5-3）One end passes through material distributing valve respectively（5-2）With 2
The individual tremie pipe（5-1）Middle part connection, 2 upper arms（5-3）The other end respectively with 2 lower branch lines（5-
4）One end connection, 2 lower branch lines（5-4）The other end be respectively equipped with the second seasoning spreading box（10）, 2 second spreadings
Box（10）It is symmetricly set on the smoke-box flue（4）On, it is arranged with the second seasoning spreading box（10）The smoke-box flue of lower section
Side wall is provided with 3 steam jets（9-1）, 3 steam jets（9-1）It is provided with the smoke-box flue sidewall of lower section
3 low NOs（14）, 3 low NOs（14）With 3 steam jets（9-1）It is downward-sloping to set
Put, the low NO（14）With the steam jet（9-1）Centrage and the dore furnace（3）Central axis between
Angle be a, a=15 °, 3 steam jets（9-1）Be arranged on smoke-box flue（4）The circulating line in outside（9-2）Connection, institute
State circulating line（9-2）By air inlet pipe and vapor catalyzed dose of tank（9-3）Connection, the vapor catalyzed dose of tank（9-3）By stream
Gauge（9-4）With control valve（9-5）With the vapour source（9-6）Connection；The low NO（14）By pipeline（15）With
Divide the connection of coal device.
2. system according to claim 1, it is characterised in that the system also includes the vapor catalyzed device of kiln hood（12）, institute
Stating the vapor catalyzed device of kiln hood includes steam jet（12-1）, vapor catalyzed dose of tank（12-2）, effusion meter（12-3）, control valve
（12-4）And vapour source（12-5）；
The steam jet（12-1）It is arranged on the rotary kiln（1）Kiln hood position, the vapor catalyzed dose of tank（12-2）'s
One end passes through pipeline and the steam jet（12-1）Connection, the vapor catalyzed dose of tank（12-2）The other end pass through the stream
Gauge（12-3）With control valve（12-4）With the vapour source（12-5）Connection, the catalyst are arranged on described vapor catalyzed dose
The catalyst is provided with tank（13）.
3. system according to claim 1 and 2, it is characterised in that first seasoning spreading box（8）With the second seasoning spreading box（10）
Structure it is identical, its structure is：Splicing plate（8-3）, spreading plate（8-4）And the charging aperture being connected with C4 tremie pipes（8-1）With
The discharging opening being connected with decomposition furnace body（8-2）, the splicing plate（8-3）With spreading plate（8-4）It is end to end, it is overall in fan
Shape, the spreading plate（8-4）In horizontally disposed, the splicing plate is in（8-3）It is obliquely installed and in the spreading plate（8-4）One
Hold affixed, the splicing plate（8-4）Inner surface be stepped, the splicing plate（8-4）Each section ladder on be equipped with pressure
Contracting air port（7）, and ladder is no less than 5 grades, the spreading plate is in horizontally disposed, the splicing plate（8-3）Each section rank
Compressed air spout is equipped with ladder（8-5）, the splicing plate bottom is provided with discloses material hole（8-6）, the spreading plate（8-3）Length
Degree is not less than 30 centimetres, and splicing plate（8-3）End is not less than 80 centimetres.
4. system according to claim 1 and 2, it is characterised in that the low NO（14）, including housing（14-
1）, jet pipe（14-2）, swirl vanes（14-3）And air inlet（14-4）；The housing（14-1）It is provided with air inlet（14-4）,
The jet pipe（14-2）It is arranged on the housing（14-1）Inside, the jet pipe（14-2）End be connected with pipeline, the rotation
Stream impeller（14-3）It is socketed in positioned at jet pipe（14-2）Front end and air inlet（14-4）Between in the jet pipe（14-2）On, it is described
Swirl vanes（14-3）Blade be twisted blade, the angle that blade distort from air intake to outlet air end be 90 °, in air intake leaf
Unilateral is 0 with axial angle, i.e., parallel with x-axis, then waits the uniform gradually transition of radian, when transitting to outlet air end, blade face
It it is 45 ° with x-axis angle.
5. system according to claim 1 and 2, it is characterised in that the smoke-box flue（4）Extend with the smoke-box flue
Pipe（11）Cross section be circle, and the smoke-box flue extension tube（11）Length be not less than 1m.
6. system according to claim 1 and 2, it is characterised in that the vapor catalyzed device of the kiln hood（9）In catalysis after
The flow that vapor is entered in dore furnace is 80-100kg/h, and the source of vapor is waste heat boiler saturated vapor, and temperature is
200-300℃。
7. system according to claim 4, it is characterised in that the jet pipe（14-2）A diameter of 20-30cm.
8. system according to claim 3, it is characterised in that the splicing plate（6）With spreading plate（5）Between angle be
150°。
9. system according to claim 1 and 2, it is characterised in that the catalyst（13）Each component quality hundred
Divide ratio：Nickel 25-30%, titanium 15-25%, chromium 5-15%, silicon 15-25%, calcium 10%, remaining as inevitable impurity.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610889311.7A CN106595294B (en) | 2016-10-11 | 2016-10-11 | Catalytic reduction method composite denitration system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610889311.7A CN106595294B (en) | 2016-10-11 | 2016-10-11 | Catalytic reduction method composite denitration system |
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| CN106595294A true CN106595294A (en) | 2017-04-26 |
| CN106595294B CN106595294B (en) | 2020-05-22 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109503008A (en) * | 2018-11-08 | 2019-03-22 | 中国中材国际工程股份有限公司 | A kind of cement clinker burning system and its without ammonia denitrating technique method |
Citations (6)
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