CN109621707A - A kind of circulating fluidized bed device and denitrating technique for industrial smoke low-temperature denitration - Google Patents
A kind of circulating fluidized bed device and denitrating technique for industrial smoke low-temperature denitration Download PDFInfo
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- CN109621707A CN109621707A CN201811558767.0A CN201811558767A CN109621707A CN 109621707 A CN109621707 A CN 109621707A CN 201811558767 A CN201811558767 A CN 201811558767A CN 109621707 A CN109621707 A CN 109621707A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
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Abstract
The present invention relates to a kind of circulating fluidized bed devices for industrial smoke low-temperature denitration, denitration reaction section: including pre-reaction section (2), reducer (3) and the conversion zone (4) being sequentially connected in series from bottom to top, the pre-reaction section (2) is for the preheating of flue gas and the premixing of flue gas and catalyst, the reducer (3) is venturi reducer pipe, and the upper end of the venturi reducer pipe is equipped with ammonia-spraying grid (6)；Bag filter: it is connected to by pipeline (12) with the top of conversion zone (4)；Returning charge transport tube (5): being set to below bag filter ash bucket (9), and the material being used between pre-reaction section (2) and bag filter ash bucket (9) is connected to and the discharge of denitrating catalyst；Catalyst storage bin (14): bottom is equipped with feed pipe (16), is connect by feed pipe (16) with pre-reaction section (2).Compared with prior art, the present invention has many advantages, such as that denitration reaction temperature is low, catalysis reaction efficiency is high and catalyst change is convenient.
Description
Technical field
The present invention relates to industrial denitrification process, more particularly, to a kind of recirculating fluidized bed for industrial smoke low-temperature denitration
Device and denitrating technique.
Background technique
Currently, existing denitrating technique is based on fixed bed SCR technique, flue gas is quickly through multi-layer honeycomb in the process flow
Formula or board-like catalyst carry out reduction reaction, and because of flue gas and catalyst contact time is short reacts insufficient in total less than 1s, and one
Divide NOxIt is easy to escape out from catalyst hole, therefore the process efficiency is not high.In addition, fixed bed catalyst uses the longevity
Life generally 3 years, more catalyst changeout needed blowing out, influences to produce.For conventional denitrification apparatus, it is required that suitable reaction range
It is 320-450 DEG C, and temperature is not suitble to add SCR denitration device for industrial and mining enterprises such as steel, carbon, glass furnaces, this
So that its denitrification process becomes problem.
CN201710469608.2 discloses a kind of combustion system of circulating fluidized bed boiler and burning process, the burning system
System includes: circulating fluidized bed boiler, has circulating flue gas outlet and secondary air inlet；Secondary air channel, the tail end of secondary air channel with
Secondary air inlet is connected, and circulating flue gas entrance is provided on secondary air channel；Circulating flue gas pipeline, one end export phase with circulating flue gas
Even, the other end is connected with circulating flue gas entrance；Reducing agent entrance, be arranged on secondary air channel, and be located at circulating flue gas entrance and
Between secondary air inlet.It joined secondary air duct in the technical solution of the invention, the residence time of reaction medium improved with this,
And for denitration reaction, improve that conversion per pass is more significant, multiple circulation will cause the volume increase of equipment with
And cost.
Summary of the invention
It is an object of the present invention to overcome the above-mentioned drawbacks of the prior art and provide one kind to be used for industrial smoke
The circulating fluidized bed device and denitrating technique of low-temperature denitration.
The purpose of the present invention can be achieved through the following technical solutions:
A kind of circulating fluidized bed device for industrial smoke low-temperature denitration, comprising: denitration reaction section: including from bottom to top
Pre-reaction section, reducer and the conversion zone being sequentially connected in series, preheating and flue gas and catalysis of the pre-reaction section for flue gas
The premixing of agent, the reducer are venturi reducer pipe, and the upper end of the venturi reducer pipe is equipped with ammonia-spraying grid, institute
Powdered denitrating catalyst is filled in the conversion zone stated；Bag filter: its top be equipped with pipeline, by pipeline with react
The top connection of section, side wall are equipped with exhanst gas outlet；Returning charge transport tube: being set to below bag filter ash bucket, is used for pre-reaction
Section is connected to the material between bag filter ash bucket and the discharge of denitrating catalyst；Catalyst storage bin: its bottom is equipped with feed
Pipe, is connect by feed pipe with pre-reaction section.
Further, the arrival end of the pre-reaction section is equipped with preheater.
Further, the feed pipe below the catalyst storage bin is equipped with frequency modulation rotary feeder, opens frequency modulation rotation
Pre-reaction section can be added in fresh catalyst after being given to glassware.
Further, the corner dimension that the injection direction of the ammonia-spraying grid and horizontal direction are in is 0 °~60 °.
Further, the bag filter includes cylindrical body of deduster, is connected to below body of deduster
Back taper ash bucket and smoke outlet tube set on body of deduster side.
Further, the middle part of returning charge transport tube is connected to the lower end of ash bucket, one end connection of returning charge transport tube
In the middle part of pre-reaction section, the other end is equipped with material outlet.
Further, the junction of the smoke outlet tube and body of deduster is equipped with strainer, the exhanst gas outlet
Pipe is equipped with air-introduced machine.
A kind of technique for industrial smoke low-temperature denitration, comprising the following steps: pre-reaction: flue gas is passed through to pre-reaction
Duan Zhong is 135 DEG C~180 DEG C by the temperature that preheater controls pre-reaction section；Venturi injection: certainly by pre-reaction section by flue gas
It is passed through in venturi reducer pipe upwards down, so that flue gas is sprayed upwards by venturi reducer pipe, and in venturi reducer pipe
Exit sprays into ammonia by ammonia-spraying grid, the NO in the ammonia and flue gasxMolar flow ratio be 0.2~0.9；Denitration
Reaction: loading denitrating catalyst into conversion zone, will pass through the flue gas of venturi reducer pipe and ammonia gas mixture body and catalyst
Contact, so that denitrating catalyst is in fluidized state；Catalyst change: the flue gas after denitration reaction is entrainment of denitrating catalyst
Enter body of deduster with the vertical direction on body of deduster top, and separated in body of deduster, will be taken off by separation
Denox catalyst is sink in ash bucket, and denitrating catalyst is back to the mixing of pre-reaction Duan Zhongyu flue gas by returning charge transport tube later, is taken off
Flue gas after nitre is discharged by the smoke outlet tube in body of deduster.
Further, the denitrating catalyst is modified V2O5-TiO2Catalyst, the modification V2O5-TiO2Catalysis
Agent is prepared by collosol and gel-infusion process and is ground to powdered.
Further, when needing replacing catalyst, the frequency modulation rotary feeder below catalyst storage bin is first opened, so that
Fresh catalyst is passed through in pre-reaction section, opens material outlet at the same time, is urged by the way of thick and thin phase burner by discarded
Agent is delivered to specified ash cellar and retains.
Compared with prior art, the invention has the following advantages that
1) it is fixed bed that catalyst, which is the fluidised and traditional SCR catalyst of powder, due to powder-type catalyst compared to
Its specific surface area of fixed bed catalyst is bigger, more reactivity sites can be provided in the reaction, so that in integrated fluidized bed
The conversion per pass of reaction is higher, reacts more abundant.
2) for the denitrating catalyst of pulverulence, what can be distributed in the reactor in fluidized state is more uniform, keeps away
The defect for having exempted from the channel generated in the reactor when using existing fixed bed catalyst and dead angle, enhances reaction process
In external diffusion process.
3) accelerate flue gas using Venturi tube in the present invention, and ammonia-spraying grid is sprayed with 0 °~60 ° of angle
It penetrates, with this ammonia of penetrating is quickly evenly distributed by the adsorption zone that rear is formed at Venturi exit, is formed with flue gas
Good dispersion also further increases the external diffusion efficiency in catalysis reaction with this.
4) denitrating catalyst powder can more fully capture the nitrogen oxides gas in flue gas in dense fluidized bed
State molecule, denitration efficiency are higher.
5) technique can supplement catalyst by material frequency modulation rotary feeder at any time, or be taken out by material outlet
And catalyst is replaced, it does not influence to produce in the process.
6) directly Industrial Stoves outlet or its waste heat boiler be followed by the device in the present invention so that device build and
Simple installation is easy, independent of large-scale heat exchange pipe network and recycle unit.
Detailed description of the invention
Fig. 1 is the structural schematic diagram in the present invention for the circulating fluidized bed device of industrial smoke low-temperature denitration.
In figure: 1, smoke inlet, 2, pre-reaction section, 3, reducer, 4, conversion zone, 5, returning charge transport tube, 6, ammonia-spraying grid,
7, material outlet, 8, body of deduster, 9, ash bucket, 10, smoke outlet tube, 11, air-introduced machine, 12, pipeline, 13, preheater, 14,
Catalyst storage bin, 15, frequency modulation rotary feeder, 16, feed pipe, the 17, first regulating valve, the 18, second regulating valve.
Specific embodiment
The present invention is described in detail with specific embodiment below in conjunction with the accompanying drawings.
Embodiment
Circulating fluidized bed device for industrial smoke low-temperature denitration includes following part:
Denitration reaction section: including pre-reaction section 2, reducer 3 and the conversion zone 4 being sequentially connected in series from bottom to top, referring to Fig. 1,
For the pre-reaction section 2 for the preheating of flue gas and the premixing of flue gas and catalyst, the reducer 3 is venturi change
Diameter pipe, the upper end of the venturi reducer pipe are equipped with ammonia-spraying grid 6, the injection direction of the ammonia-spraying grid 6 and level side
The corner dimension of Xiang Suocheng is 0~60 °.Powdered denitrating catalyst is filled in the conversion zone 4, the denitration is urged
Agent is modified V2O5-TiO2Catalyst, modification V2O5-TiO2Catalyst is prepared by collosol and gel-infusion process and is ground to powder
Last shape, 2 arrival end of pre-reaction section are equipped with preheater 13.
Bag filter: its top is equipped with pipeline 12, is connected to by pipeline 12 with the top of conversion zone 4, side wall is equipped with
Exhanst gas outlet 10.Referring to Fig. 1, the bag filter includes cylindrical body of deduster 8, is connected to body of deduster 8
The ash bucket 9 of the back taper of lower section and smoke outlet tube 10 set on 8 side of body of deduster.The smoke outlet tube 10 with remove
The junction of dirt device ontology 8 is equipped with strainer, and the smoke outlet tube 10 is equipped with air-introduced machine 11.
Returning charge transport tube 5: it is set to 9 lower section of bag filter ash bucket, between pre-reaction section 2 and bag filter ash bucket 9
Material connection and the discharge of denitrating catalyst, the middle part of the returning charge transport tube 5 is connected to the lower end of ash bucket 9, returning charge
One end of transport tube 5 is connected to the middle part of pre-reaction section 2, and the other end is equipped with material outlet 7.
Catalyst storage bin 14: its bottom is equipped with feed pipe 16, is connect by feed pipe 16 with pre-reaction section 2.Catalyst storage
The feed pipe 16 of 14 lower section of storehouse is equipped with frequency modulation rotary feeder 15, can be by fresh catalyst after unlatching frequency modulation rotary feeder 15
Pre-reaction section 2 is added.
The device is during specific running:
First by Industrial Stoves outlet or its waste heat boiler be followed by the smoke inlet 1 in the present invention, later by flue gas into
Enter into pre-reaction section 2, by preheater 13 control pre-reaction section 2 temperature be 135 DEG C~180 DEG C, in pre-reaction section 2 with
The denitrating catalyst powder mixing that returning charge transport tube 5 returns, so that denitrating catalyst is preheated to reaction temperature in flue gas, by cigarette
Gas is passed through in venturi reducer pipe by pre-reaction section 2 is bottom-up, so that flue gas is sprayed upwards by venturi reducer pipe, and
The exit of venturi reducer pipe sprays into ammonia by ammonia-spraying grid 6, the NO in the ammonia and flue gasxMolar flow ratio
It is 0.2~0.9, ammonia-spraying grid is sprayed when injection with 0 °~60 ° of angle specifically, is made at Venturi exit with this
The ammonia of penetrating is quickly evenly distributed by the adsorption zone that rear is formed, and forms good dispersion with flue gas, is also further mentioned with this
External diffusion efficiency in height catalysis reaction.
During fluidized reaction: being filled with modified V in conversion zone 4 in advance2O5-TiO2Catalyst, the catalyst
It is prepared by collosol and gel-infusion process and is ground to powdered.By by the flue gas of venturi reducer pipe and ammonia gas mixture body with
Catalyst contact, so that denitrating catalyst is in fluidized state, what can be distributed in the reactor in fluidized state is more uniform, keeps away
The defect for having exempted from turbulent flow and dead angle that existing fixed bed catalyst generates in the reactor, enhances extending out in reaction process
The process of dissipating.
Finally carry out the separation and recycling of catalyst fines: flue gas after denitration reaction entrainment of denitrating catalyst with
The vertical direction on 8 top of body of deduster enters body of deduster 8, and is separated in body of deduster 8, by denitrating catalyst
It is sink in ash bucket 9, and flue gas is discharged by the smoke outlet tube 10 in body of deduster 8, the second regulating valve 18, which is in, at this time opens
State, denitrating catalyst is back in pre-reaction section 2 by returning charge transport tube 5 and is mixed with flue gas later.It is catalyzed when needing replacing
When agent, the first regulating valve 17 of 7 side of material outlet is first opened, so that catalyst to be replaced is discharged by material outlet 7, and is adopted
Waste catalyst is delivered to specified ash cellar with the mode of thick and thin phase burner to retain, the first regulating valve 17 is closed later and opens
Second regulating valve 18, and the frequency modulation rotary feeder 15 of 14 lower section of catalyst storage bin is opened simultaneously, so that fresh catalyst is passed through
In pre-reaction section 2.
Claims (9)
1. a kind of circulating fluidized bed device for industrial smoke low-temperature denitration characterized by comprising
Denitration reaction section: described including pre-reaction section (2), reducer (3) and the conversion zone (4) being sequentially connected in series from bottom to top
For pre-reaction section (2) for the preheating of flue gas and the premixing of flue gas and catalyst, the reducer (3) is venturi variable diameter
The upper end of pipe, the venturi reducer pipe is equipped with ammonia-spraying grid (6), and powdered take off is filled in the conversion zone (4)
Denox catalyst；
Bag filter: its top is equipped with pipeline (12), is connected to by pipeline (12) with the top of conversion zone (4), is set on side wall
There are exhanst gas outlet (10)；
Returning charge transport tube (5): being set to below bag filter ash bucket (9), for pre-reaction section (2) and bag filter ash bucket
(9) material connection and the discharge of denitrating catalyst between；
Catalyst storage bin (14): its bottom is equipped with feed pipe (16), is connect by feed pipe (16) with pre-reaction section (2).
2. a kind of circulating fluidized bed device for industrial smoke low-temperature denitration according to claim 1, which is characterized in that
The arrival end of the pre-reaction section (2) is equipped with preheater (13).
3. a kind of circulating fluidized bed device for industrial smoke low-temperature denitration according to claim 1, which is characterized in that
The corner dimension that the injection direction and horizontal direction of the ammonia-spraying grid (6) are in is 0 °~60 °.
4. a kind of circulating fluidized bed device for industrial smoke low-temperature denitration according to claim 1, which is characterized in that
The bag filter includes the ash of cylindrical body of deduster (8), the back taper being connected to below body of deduster (8)
Struggle against (9) and be set to the smoke outlet tube (10) of body of deduster (8) side.
5. a kind of circulating fluidized bed device for industrial smoke low-temperature denitration according to claim 4, which is characterized in that
The middle part of the returning charge transport tube (5) is connected to the lower end of ash bucket (9), and one end of returning charge transport tube (5) is connected to pre-reaction
The middle part of section (2), the other end are equipped with material outlet (7).
6. a kind of circulating fluidized bed device for industrial smoke low-temperature denitration according to claim 4, which is characterized in that
The junction of the smoke outlet tube (10) and body of deduster (8) is equipped with strainer, and the smoke outlet tube is set on (10)
There are air-introduced machine (11).
7. a kind of technique for industrial smoke low-temperature denitration, which comprises the following steps:
Pre-reaction: flue gas is passed through into pre-reaction section (2), and the temperature by preheater (13) control pre-reaction section (2) is 135
DEG C~180 DEG C；
Venturi injection: flue gas is passed through in venturi reducer pipe by pre-reaction section (2) is bottom-up, so that flue gas passes through literary mound
In reducer pipe spray upwards, and the exit of venturi reducer pipe by ammonia-spraying grid (6) spray into ammonia, the ammonia with
NO in flue gasxMolar flow ratio be 0.2~0.9；
Denitration reaction: to denitrating catalyst is loaded in conversion zone (4), the flue gas and ammonia gas mixture of venturi reducer pipe will be passed through
Body is contacted with catalyst, so that denitrating catalyst is in fluidized state；
Catalyst change: the flue gas after denitration reaction is entrainment of denitrating catalyst with the vertical of body of deduster (8) top
Direction enters body of deduster (8), and is separated in body of deduster (8), and denitrating catalyst is sink to ash bucket by separating
(9) in, denitrating catalyst is back in pre-reaction section (2) by returning charge transport tube (5) and is mixed with flue gas later, the cigarette after denitration
Gas is discharged by the smoke outlet tube (10) on body of deduster (8).
8. a kind of technique for industrial smoke low-temperature denitration according to claim 7, which is characterized in that the denitration
Catalyst is modified V2O5-TiO2Catalyst, the modification V2O5-TiO2Catalyst is prepared and is ground by collosol and gel-infusion process
Mill is powdered.
9. a kind of technique for industrial smoke low-temperature denitration according to claim 7, which is characterized in that when needing replacing
When catalyst, material outlet (7) first are opened, waste catalyst is delivered to specified ash cellar by the way of thick and thin phase burner and is stayed
It deposits, the frequency modulation rotary feeder (15) below catalyst storage bin (14) is opened later, so that fresh catalyst is passed through pre-reaction section
(2) in.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811558767.0A CN109621707A (en) | 2018-12-19 | 2018-12-19 | A kind of circulating fluidized bed device and denitrating technique for industrial smoke low-temperature denitration |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811558767.0A CN109621707A (en) | 2018-12-19 | 2018-12-19 | A kind of circulating fluidized bed device and denitrating technique for industrial smoke low-temperature denitration |
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| CN109621707A true CN109621707A (en) | 2019-04-16 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111545049A (en) * | 2020-04-29 | 2020-08-18 | 南京赤博环保科技有限公司 | SNCR (Selective non catalytic reduction) denitration system and method for removing escaping ammonia in SNCR denitration process |
| CN115350587A (en) * | 2022-08-09 | 2022-11-18 | 攀枝花市蓝鼎环保科技有限公司 | Circulating fluidized bed device for low-temperature denitration of industrial flue gas and denitration process thereof |
-
2018
- 2018-12-19 CN CN201811558767.0A patent/CN109621707A/en active Pending
Non-Patent Citations (1)
| Title |
|---|
| 张建良 等编著: "《非高炉炼铁》", 31 March 2015 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111545049A (en) * | 2020-04-29 | 2020-08-18 | 南京赤博环保科技有限公司 | SNCR (Selective non catalytic reduction) denitration system and method for removing escaping ammonia in SNCR denitration process |
| CN115350587A (en) * | 2022-08-09 | 2022-11-18 | 攀枝花市蓝鼎环保科技有限公司 | Circulating fluidized bed device for low-temperature denitration of industrial flue gas and denitration process thereof |
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