CN110152486A - Flue gas denitrification system - Google Patents
Flue gas denitrification system Download PDFInfo
- Publication number
- CN110152486A CN110152486A CN201910476422.9A CN201910476422A CN110152486A CN 110152486 A CN110152486 A CN 110152486A CN 201910476422 A CN201910476422 A CN 201910476422A CN 110152486 A CN110152486 A CN 110152486A
- Authority
- CN
- China
- Prior art keywords
- catalyst module
- flue gas
- ammonia
- reactor body
- ammonium hydroxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 77
- 239000003546 flue gas Substances 0.000 title claims abstract description 77
- 239000003054 catalyst Substances 0.000 claims abstract description 98
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 66
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 33
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000000908 ammonium hydroxide Substances 0.000 claims abstract description 32
- 239000004071 soot Substances 0.000 claims abstract description 23
- 238000007664 blowing Methods 0.000 claims abstract description 19
- 238000005507 spraying Methods 0.000 claims abstract description 19
- 239000003463 adsorbent Substances 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 238000003860 storage Methods 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 16
- 230000008676 import Effects 0.000 claims description 15
- 239000000571 coke Substances 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 6
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 230000004048 modification Effects 0.000 claims description 4
- 238000012986 modification Methods 0.000 claims description 4
- 239000006260 foam Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 229910052759 nickel Inorganic materials 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 239000000758 substrate Substances 0.000 claims description 3
- 210000003850 cellular structure Anatomy 0.000 claims 1
- 239000003610 charcoal Substances 0.000 claims 1
- 229910000831 Steel Inorganic materials 0.000 abstract description 8
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 239000010959 steel Substances 0.000 abstract description 8
- 238000010276 construction Methods 0.000 abstract description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 12
- 238000000034 method Methods 0.000 description 8
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 230000009471 action Effects 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 235000019504 cigarettes Nutrition 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000013517 stratification Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 235000012204 lemonade/lime carbonate Nutrition 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000000644 propagated effect Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000035882 stress Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8628—Processes characterised by a specific catalyst
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The present invention relates to a kind of flue gas denitrification systems.It includes tank used for storing ammonia, ammonium hydroxide delivery pump, ammonium hydroxide evaporator tank, tar adsorbent equipment, hot-blast stove, ammonia-spraying grid, reactor body, deflector, flow straightening grid, the first catalyst module, the second catalyst module, preparing catalyst module, sonic soot blowing device and compressor storage tank.A kind of flue gas denitrification system of the present invention, hot-blast stove provide hot-air preheating catalyst module for reactor body, ensure that the service life of catalyst module, while but also reactor body internal-external temperature difference is little, preventing steel construction from deforming；It is urged by the temperature difference of the heating rate of control catalyst module, flue gas and catalyst module and flue gas heating rate prevents catalyst structure from damaging；Ammonia is mixed with the abundant, uniform of flue gas using ammonia-spraying grid, and catalyst module is periodically purged and cleaned using sonic soot blowing device, ensure that the efficiency of denitration reaction.
Description
Technical field
The present invention relates to a kind of flue gas denitrification system more particularly to a kind of denitrating systems for coke oven flue gas.Belong to cigarette
Gas disposal technical field.
Background technique
Coking industry is the important component of Chemical Industry, while being also that the important upstream industry of steel industry is held
Industry, extensive development all the time produce serious influence to ecological environment, wherein coke oven heating generate sulfur dioxide and
Nitrogen oxides, when atmosphere pollution one of pollution sources, therefore control sulfur dioxide and nitrogen oxides discharge be coking industry face
The significant task faced.
Wet desulphurization when the main sulfur removal technology in China at present, mainly use lime stone, lime or sodium carbonate etc. as
Detergent washs flue gas in desulfurizing tower, to remove the sulfur dioxide in flue gas.
Denitrating technique mainly selective non-catalytic reduction (SNCR) technique and selective catalytic reduction (SCR) technique.Its
Middle SNCR denitration technique is to spray into reducing agent in the temperature window for being suitble to denitration reaction without using catalyst,
Nitrogen oxides in flue gas is reduced to harmless nitrogen and water, due to the limitation of reaction temperature window and leakage ammonia, denitration efficiency
More generally 30~50%, for large-sized station boiler, denitration efficiency is generally below 40%.And SCR denitrating technique is certain
Temperature and catalyst under the action of, using ammonia as reducing agent, the nitrogen oxides in flue gas is optionally reduced to nitrogen
The technique of gas and water.Without byproduct, by larger catalyst loadings, denitration efficiency can reach 80% or more, in SCR denitration work
In skill, flue-gas temperature is the important parameter of selecting catalyst, and SCR denitration technology needs carry out in certain temperature section, simultaneously
There are the optimum temperatures of catalysis.SCR denitration excellent in efficiency, generally 80% or more, therefore the fume treatment of capacity coke oven is adopted mostly
Use SCR denitration process.
Existing flue gas denitrification system has the following problems: 1, when reactor in the cold state start, catalyst module itself
Temperature it is very low, if ammoniated at this time, a large amount of hydrogen sulfate ammonia can be generated, and condense in catalyst pores, substantially reduce and urge
The activity of agent, if often operation in this way, will seriously reduce the service life of catalyst module；2, entire reactor is steel construction
Production, inside are equipped with the facilities such as many supporting beams, if the rising of catalyst module temperature is too fast, cause internal-external temperature difference excessive,
It will lead to the deformation of steel construction；3, catalyst module temperature rise is more than maximum allowable temperature rise, and the moisture condensed in catalyst will
Evaporation suddenly generates the effect of similar explosion, and heat can also be generated by damaging catalyst structure if catalyst internal-external temperature difference is excessive
Stress damage；4, using the time it is longer after, have dust stratification on the catalyst module in reactor, dust stratification can increase gas-flow resistance, shadow
Ring the efficiency of denitration reaction.
Summary of the invention
The purpose of the present invention is to overcome the above shortcomings and to provide a kind of flue gas denitrification systems.
The object of the present invention is achieved like this:
A kind of flue gas denitrification system, its main feature is that: it includes tank used for storing ammonia, ammonium hydroxide delivery pump, ammonium hydroxide evaporator tank, tar suction
Adsorption device, hot-blast stove, ammonia-spraying grid, reactor body, deflector, flow straightening grid, the first catalyst module, the second catalyst mould
Block, preparing catalyst module, sonic soot blowing device and compressor storage tank；
The ammonium hydroxide of 20% concentration is filled in tank used for storing ammonia, the outlet of tank used for storing ammonia and the import of ammonium hydroxide delivery pump connect, ammonia
The outlet of water delivery pump is connect with the import of ammonium hydroxide evaporator tank, and the outlet of ammonium hydroxide evaporator tank and the ammonia imports of ammonia-spraying grid connect
It connects；
The exhaust outlet of coke oven flue gas is connect with the import of tar adsorbent equipment；
Hot-blast stove setting connects in coke oven flue gas exit, the outlet of tar adsorbent equipment and the gas inlet of ammonia-spraying grid
It connects；
The top of reactor body is arranged in deflector, and deflector is diagonally disposed；
The top of reactor body is arranged in flow straightening grid, and is located at the lower section of deflector；
First catalyst module, the second catalyst module and preparing catalyst module are from top to bottom successively set on reactor
The middle part of ontology；The side of reactor body is arranged in sonic soot blowing device, and the first catalyst module is at least corresponding, and there are three sound
Wave soot blower, the second catalyst module is at least corresponding there are three sonic soot blowing device, and compression gas storage tank is located at reactor body
Outside, the import of the outlet access sonic soot blowing device of compressor storage tank.
Further, the heating rate of the first catalyst module, the second catalyst module and preparing catalyst module does not surpass
100 DEG C/min is crossed, and the temperature difference between flue gas and catalyst module is no more than 150 DEG C, during startup, works as flue-gas temperature
When lower than water dew point, flue gas temperature rise control is in 5 DEG C/min, and after flue-gas temperature is higher than water dew point, flue gas temperature rise is increased to 50-
60℃/min。
Further, awning is provided at the top of reactor body.
Further, the first catalyst module, the second catalyst module and preparing catalyst module use high temperature modification honeycomb
Formula structure.
Further, the material composition of the first catalyst module, the second catalyst module and preparing catalyst module with
V2O5 is active component, and TiO2 is substrate.
Further, tar adsorbent equipment includes the coke on upper layer and the nickel foam metal screen of lower layer.
Compared with prior art, the beneficial effects of the present invention are:
1, a kind of flue gas denitrification system of the present invention, when reactor starts in the cold state, the temperature of catalyst module itself is very
Low, hot-blast stove provides hot-air for reactor body at this time, and hot-air preheating catalyst module ensure that making for catalyst module
With the service life, while but also reactor body internal-external temperature difference is little, prevent steel construction from deforming.
2, a kind of flue gas denitrification system of the present invention, the heating rate of catalyst module must not exceed 100 DEG C/min, and flue gas
The temperature difference between catalyst module is no more than 150 DEG C, generally during startup, when flue-gas temperature is lower than water dew point, cigarette
Temperature liter ought be controlled in 5 DEG C/min, and after flue-gas temperature is higher than water dew point, 50-60 DEG C/min is can be improved in flue gas temperature rise,
Therefore the moisture condensed in catalyst module will not evaporate suddenly, prevent catalyst structure from damaging.
3, a kind of flue gas denitrification system of the present invention, is mixed ammonia with the abundant, uniform of flue gas using ammonia-spraying grid, and adopt
Catalyst module is periodically purged and cleaned with sonic soot blowing device, ensure that the efficiency of denitration reaction.
Detailed description of the invention
Fig. 1 is a kind of flow chart of flue gas denitrification system of the present invention.
The specific schematic diagram of reactor body Fig. 2 of the invention.
Fig. 3 is the left view of Fig. 2.
In figure:
Reactor body 1, ammonia-spraying grid 2, deflector 3, flow straightening grid 4, the first catalyst module 5, the second catalyst mould
Block 6, preparing catalyst module 7, sonic soot blowing device 8, compression gas storage tank 9, awning 10, tank used for storing ammonia 11, ammonium hydroxide delivery pump 12,
Ammonium hydroxide evaporator tank 13, tar adsorbent equipment 14, hot-blast stove 15.
Specific embodiment
With reference to the accompanying drawings and examples, further description of the specific embodiments of the present invention.Following embodiment is only
For clearly illustrating technical solution of the present invention, and not intended to limit the protection scope of the present invention.
Referring to Fig. 1, the present invention relates to a kind of flue gas denitrification systems, it includes tank used for storing ammonia 11, ammonium hydroxide delivery pump 12, ammonium hydroxide
Evaporator tank 13, tar adsorbent equipment 14, hot-blast stove 15, ammonia-spraying grid 2 and reactor body 1；
The ammonium hydroxide of 20% concentration is passed through in tank used for storing ammonia 11, the outlet of tank used for storing ammonia 11 and the import of ammonium hydroxide delivery pump 12 connect
It connects, the outlet of ammonium hydroxide delivery pump 12 is connect with the import of ammonium hydroxide evaporator tank 13, the outlet of ammonium hydroxide evaporator tank 13 and ammonia-spraying grid
Ammonia imports connection, for ammonium hydroxide evaporator tank 13 under the action of hot wind, ammonium hydroxide evaporates into ammonia-spraying grid；
The exhaust outlet of coke oven flue gas is connect with the import of tar adsorbent equipment 14, and tar adsorbent equipment 14 includes upper layer
Coke and lower layer nickel foam metal screen, coke is a kind of porous structure, it is possible to provide very big surface area, and have very
Strong adsorption capacity, by the suction-operated of capillary, to remove impurity most in flue gas；
Hot-blast stove 15 is arranged in coke oven flue gas exit, and in the case where flue-gas temperature is relatively low, hot-blast stove 15 adds for flue gas
Heat, by flue-gas temperature control in 280 DEG C or more (300-320 DEG C), hot-blast stove 15 or catalyst module preheating；
The outlet of tar adsorbent equipment 14 is connect with the gas inlet of ammonia-spraying grid 2, and the flue gas of ammonia and tar removing is spraying
Ammonia grid 2 converges, and under the action of ammonia-spraying grid 2, ammonia is mixed with the abundant, uniform of flue gas；
Referring to figure 2-3, the top of reactor body 1 is arranged in deflector 3, and deflector 3 is diagonally disposed, is ammonia and flue gas
Mixed airflow provide guiding role；
Flow straightening grid 4 is arranged in the top of reactor body 1, and is located at the lower section of deflector 3, and flow straightening grid 4 is by ammonia
Mixing with flue gas gas is to flow straight down, while mixed gas is touched in flow straightening grid 4 by horizontal direction flow adjustment
It hits, integrate, the VELOCITY DISTRIBUTION of mixed gas is integrated relatively uniform；
First catalyst module 5, the second catalyst module 6, preparing catalyst module 7 are from top to bottom successively set on reaction
The middle part of device ontology 1；First catalyst module 5, the second catalyst module 6, preparing catalyst module 7 are cellular using high temperature modification
Structure, for the material composition used using V2O5 as active component, TiO2 is substrate；
The side of reactor body 1 is arranged in sonic soot blowing device 8, and the first catalyst module 5 is at least corresponding, and there are three sound
Wave soot blower 8, the second catalyst module 6 is at least corresponding there are three sonic soot blowing device 8, and preparing catalyst module 7 is reserved to be opened；
The mouthpiece of sonic soot blowing device 8 is arranged in reactor body 1, and compression gas storage tank 9 is located at outside reactor body 1, compressor storage
The import of the outlet access sonic soot blowing device 8 of tank 9, sonic soot blowing device 8 are limited using instrument and meter for automation prosperous in Liaoning
The SQ-160 type acoustic wave soot blower of company's production.
Purging and cleaning of the sonic soot blowing device 8 for catalyst module, its working principle is that being to convert compressed air
It is sent into reactor body 1, urges at high-power sound wave (a kind of pressure wave propagated in space medium in the form of dilatational wave)
When dust stratification in agent module is drawn repeatedly by the dilatational wave alternately changed with certain frequency, pressure acts on, fall off because fatigue is loose,
It takes away with flue gas stream, or sinks under the effect of gravity.
Since entire Benitration reactor is structure steel fabrication, inside is equipped with the facilities such as many supporting beams, if catalyst mould
Deblocking temperature rising is too fast, causes internal-external temperature difference excessive, also results in the deformation of steel construction；Once in addition, catalyst module temperature rise
More than maximum allowable temperature rise, the moisture condensed in catalyst module will evaporate suddenly, generate the effect of similar explosion, damage
Catalyst module structure can also generate thermal stress damage, therefore of the invention first if catalyst module internal-external temperature difference is excessive
Catalyst module 5, the second catalyst module 6, the heating rate of preparing catalyst module 7 must not exceed 100 DEG C/min, and cigarette
The temperature difference between gas and catalyst module is no more than 150 DEG C.Generally during startup, when flue-gas temperature is lower than water dew point,
Flue gas temperature rise ought be controlled in 5 DEG C/min, after flue-gas temperature is higher than water dew point, flue gas temperature rise can be improved 50-60 DEG C/
min。
The top of reactor body 1 is additionally provided with awning 10, and awning can prevent sleet disturbing reaction device sheet in rain and snow
1 surface temperature of body, to influence the operating temperature in reactor body 1.
Working principle:
Under the action of ammonium hydroxide delivery pump 12, the ammonium hydroxide of 20% concentration enters ammonium hydroxide evaporator tank 13 from tank used for storing ammonia 11,
It is heated by high temperature dilution wind by ammonium hydroxide heating evaporation, while by ammonia concentration in ammonium hydroxide evaporator tank 13 and is diluted to 5%, in this way
Ammonia/air mixture is safe and nonflammable, and ammonium hydroxide evaporates into ammonia-spraying grid 2；(220-320 DEG C) of the flue gas warp come out from coke oven
Hot-blast stove 15 enters tar adsorbent equipment 14 after heating, most miscellaneous in flue gas under the action of tar adsorbent equipment 14
Matter is removed, and the flue gas and ammonia after removing impurity converge in ammonia-spraying grid 2, and ammonia sufficiently, after evenly mixing enters with flue gas
In reactor body 1, deflector 3 mixes with flue gas air-flow for ammonia and provides guiding role, under the action of flow straightening grid 4,
It is to flow straight down, while the VELOCITY DISTRIBUTION of mixed gas is whole by horizontal direction flow adjustment that ammonia, which mixes with flue gas gas,
Close relatively uniform；Then the mixed gas of ammonia and flue gas passes sequentially through the first catalyst module 5, the second catalyst module 6
With preparing catalyst module 7, the reduction of NOx and removal are realized, each catalyst module dust stratification is more when causing gas-flow resistance, sound
Wave soot blower 8 is purged and is cleaned to it.
A kind of flue gas denitrification system of the present invention, when reactor starts in the cold state, the temperature of catalyst module itself is very low,
Hot-blast stove 15 is that reactor body 1 provides hot-air at this time, and hot-air preheating catalyst module ensure that making for catalyst module
With the service life, while but also 1 internal-external temperature difference of reactor body is little, prevent steel construction from deforming.
A kind of flue gas denitrification system of the present invention, the heating rate of catalyst module must not exceed 100 DEG C/min, and flue gas
The temperature difference between catalyst module is no more than 150 DEG C, generally during startup, when flue-gas temperature is lower than water dew point, cigarette
Temperature liter ought be controlled in 5 DEG C/min, and after flue-gas temperature is higher than water dew point, 50-60 DEG C/min is can be improved in flue gas temperature rise,
Therefore the moisture condensed in catalyst module will not evaporate suddenly, prevent catalyst structure from damaging
A kind of flue gas denitrification system of the present invention, is mixed ammonia with the abundant, uniform of flue gas using ammonia-spraying grid 2, and adopt
Catalyst module is periodically purged and cleaned with sonic soot blowing device 8, ensure that the efficiency of denitration reaction.
In the above-described embodiments, exemplary description only is carried out to the present invention, but those skilled in the art are originally special in reading
The present invention can be carry out various modifications without departing from the spirit and scope of the present invention after benefit application.
Claims (6)
1. a kind of flue gas denitrification system, it is characterised in that: it includes tank used for storing ammonia, ammonium hydroxide delivery pump, ammonium hydroxide evaporator tank, tar suction
Adsorption device, hot-blast stove, ammonia-spraying grid, reactor body, deflector, flow straightening grid, the first catalyst module, the second catalyst mould
Block, preparing catalyst module, sonic soot blowing device and compressor storage tank；
The ammonium hydroxide of 20% concentration is filled in tank used for storing ammonia, the outlet of tank used for storing ammonia and the import of ammonium hydroxide delivery pump connect, and ammonium hydroxide is defeated
The outlet of pump and the import of ammonium hydroxide evaporator tank is sent to connect, the outlet of ammonium hydroxide evaporator tank and the ammonia imports of ammonia-spraying grid connect；
The exhaust outlet of coke oven flue gas is connect with the import of tar adsorbent equipment；
Hot-blast stove setting is connected in coke oven flue gas exit, the outlet of tar adsorbent equipment and the gas inlet of ammonia-spraying grid；
The top of reactor body is arranged in deflector, and deflector is diagonally disposed；
The top of reactor body is arranged in flow straightening grid, and is located at the lower section of deflector；
First catalyst module, the second catalyst module and preparing catalyst module are from top to bottom successively set on reactor body
Middle part；The side of reactor body is arranged in sonic soot blowing device, and the first catalyst module is at least corresponding to be blown there are three sound wave
Apparatus for ash, the second catalyst module is at least corresponding there are three sonic soot blowing device, and compression gas storage tank is located at outside reactor body, presses
The import of the outlet access sonic soot blowing device of contracting device storage tank.
2. a kind of flue gas denitrification system according to claim 1, it is characterised in that: the first catalyst module, the second catalysis
The heating rate of agent module and preparing catalyst module is no more than 100 DEG C/min, and the temperature difference between flue gas and catalyst module
No more than 150 DEG C, during startup, when flue-gas temperature is lower than water dew point, flue gas temperature rise is controlled in 5 DEG C/min, works as flue gas
After temperature is higher than water dew point, flue gas temperature rise is increased to 50-60 DEG C/min.
3. a kind of flue gas denitrification system according to claim 1, it is characterised in that: the top of reactor body is arranged rainy
Canopy.
4. a kind of flue gas denitrification system according to claim 1, it is characterised in that: the first catalyst module, the second catalysis
Agent module and preparing catalyst module use high temperature modification cellular structure.
5. a kind of flue gas denitrification system according to claim 1, it is characterised in that: the first catalyst module, the second catalysis
For the material composition of agent module and preparing catalyst module using V2O5 as active component, TiO2 is substrate.
6. a kind of flue gas denitrification system according to claim 1, it is characterised in that: tar adsorbent equipment includes the coke on upper layer
The nickel foam metal screen of charcoal and lower layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910476422.9A CN110152486A (en) | 2019-06-03 | 2019-06-03 | Flue gas denitrification system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910476422.9A CN110152486A (en) | 2019-06-03 | 2019-06-03 | Flue gas denitrification system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110152486A true CN110152486A (en) | 2019-08-23 |
Family
ID=67627309
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910476422.9A Pending CN110152486A (en) | 2019-06-03 | 2019-06-03 | Flue gas denitrification system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110152486A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111939744A (en) * | 2020-07-22 | 2020-11-17 | 珠海映创新能源科技有限公司 | Biomass boiler denitration system and biomass boiler denitration process |
| CN112275137A (en) * | 2020-09-21 | 2021-01-29 | 东方电气集团东方锅炉股份有限公司 | System and method for preheating sintering flue gas SCR denitration catalyst |
| CN113813755A (en) * | 2021-08-25 | 2021-12-21 | 华能沁北发电有限责任公司 | Denitration full-load commissioning control method for coal-fired unit |
| CN114210197A (en) * | 2021-11-09 | 2022-03-22 | 北京京仪自动化装备技术股份有限公司 | Exhaust gas treatment system |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07299331A (en) * | 1994-05-10 | 1995-11-14 | Mitsui Mining Co Ltd | Dry desulfurization and denitration process |
| CN101439260A (en) * | 2008-12-04 | 2009-05-27 | 浙江大学 | System for removing nitrous oxides in low-temperature flue gas and technique thereof |
| CN202893191U (en) * | 2012-11-21 | 2013-04-24 | 江苏中建材环保研究院有限公司 | Novel SCR (selective catalytic reduction)de-nitration catalyst preheater |
| CN104190253A (en) * | 2014-08-25 | 2014-12-10 | 上海宝钢节能环保技术有限公司 | Coke oven flue gas SCR denitration system |
| CN205164505U (en) * | 2015-10-22 | 2016-04-20 | 中国石油化工股份有限公司 | Boiler flue gas selectivity catalysis denitrification facility |
| CN106310933A (en) * | 2016-08-24 | 2017-01-11 | 中科科林（辽宁）能源环保有限公司 | Flue gas denitration system for coal water slurry boiler and method for denitrating flue gas |
| CN107020013A (en) * | 2016-02-01 | 2017-08-08 | 北京亚太环保股份有限公司 | A kind of low-temperature denitrifying system |
-
2019
- 2019-06-03 CN CN201910476422.9A patent/CN110152486A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07299331A (en) * | 1994-05-10 | 1995-11-14 | Mitsui Mining Co Ltd | Dry desulfurization and denitration process |
| CN101439260A (en) * | 2008-12-04 | 2009-05-27 | 浙江大学 | System for removing nitrous oxides in low-temperature flue gas and technique thereof |
| CN202893191U (en) * | 2012-11-21 | 2013-04-24 | 江苏中建材环保研究院有限公司 | Novel SCR (selective catalytic reduction)de-nitration catalyst preheater |
| CN104190253A (en) * | 2014-08-25 | 2014-12-10 | 上海宝钢节能环保技术有限公司 | Coke oven flue gas SCR denitration system |
| CN205164505U (en) * | 2015-10-22 | 2016-04-20 | 中国石油化工股份有限公司 | Boiler flue gas selectivity catalysis denitrification facility |
| CN107020013A (en) * | 2016-02-01 | 2017-08-08 | 北京亚太环保股份有限公司 | A kind of low-temperature denitrifying system |
| CN106310933A (en) * | 2016-08-24 | 2017-01-11 | 中科科林（辽宁）能源环保有限公司 | Flue gas denitration system for coal water slurry boiler and method for denitrating flue gas |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111939744A (en) * | 2020-07-22 | 2020-11-17 | 珠海映创新能源科技有限公司 | Biomass boiler denitration system and biomass boiler denitration process |
| CN112275137A (en) * | 2020-09-21 | 2021-01-29 | 东方电气集团东方锅炉股份有限公司 | System and method for preheating sintering flue gas SCR denitration catalyst |
| CN113813755A (en) * | 2021-08-25 | 2021-12-21 | 华能沁北发电有限责任公司 | Denitration full-load commissioning control method for coal-fired unit |
| CN113813755B (en) * | 2021-08-25 | 2023-11-28 | 华能沁北发电有限责任公司 | Control method for full-load operation of denitrification units for coal-fired units |
| CN114210197A (en) * | 2021-11-09 | 2022-03-22 | 北京京仪自动化装备技术股份有限公司 | Exhaust gas treatment system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110152486A (en) | Flue gas denitrification system | |
| CN206508772U (en) | Cat ceramic fiber filter pipe flue gas desulfurization and dedusting denitrification integrated device | |
| CN106861350A (en) | The biomass electric power plant gas cleaning handling process and system of dry desulfurization and low-temperature denitration | |
| CN202478804U (en) | Sintering machine flue gas desulphurization denitration device | |
| CN105944564A (en) | Coke oven flue gas waste heat recycling, desulfurization and denitration integrated system and method | |
| CN103406006A (en) | SCR (Selective Catalytic Reduction) denitration device for NOx control of rotary cement kiln | |
| CN203355611U (en) | Device for removing NOX and dioxins in sintering and pelletizing flue gas through SCR (Selective Catalytic Reduction) | |
| CN108837677A (en) | A kind for the treatment of process and its device of sintering flue gas minimum discharge | |
| CN111821852A (en) | A combined removal device and process for carbon monoxide and nitrogen oxides from sintering flue gas | |
| CN203494378U (en) | SCR (Selective Catalytic Reduction) denitration device for controlling NOx of rotary cement kiln | |
| CN102909104B (en) | Thermal regeneration method and device of SCR (selective catalytic reduction) denitration catalyst | |
| CN111589288A (en) | Desulfurization, denitrification and white removal device for ultralow emission of flue gas of sintering machine and process thereof | |
| CN208839374U (en) | A kind of middle low-temperature smoke air SCR denitrification apparatus of cement producing line | |
| CN113446865A (en) | Ceramic catalyst desulfurization, denitrification and dust removal integrated process | |
| CN110833755A (en) | System and method for removing white and nitrate after sintering flue gas wet desulphurization | |
| CN201754034U (en) | Comprehensive treatment system for glass furnace flue gas | |
| CN211936312U (en) | Blast furnace hot blast stove waste gas desulfurization denitration system | |
| CN212262910U (en) | Ultra-clean discharge system for desulfurization, denitrification and waste heat recovery of coke oven flue gas | |
| CN212236736U (en) | A combined removal device for carbon monoxide and nitrogen oxides from sintering flue gas | |
| CN211936311U (en) | Gas power generation boiler waste gas desulfurization and denitrification system | |
| CN202845023U (en) | Heat treatment regeneration device of SCR (Selective Catalytic Reduction) denitration catalyst | |
| CN111715068A (en) | Ultra-clean discharge system and method for desulfurization, denitrification and waste heat recycling of coke oven flue gas | |
| CN207734844U (en) | Middle and low temperature flue gas dust removal denitration integrated device | |
| CN217015752U (en) | Integrated treatment system for desulfurization, denitration and dust removal of calcined flue gas | |
| CN212039464U (en) | A system for dedusting and desulfurization of CDQ discharge gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190823 |