CN109966919A - The device and method of catalyst sections on-line regeneration in SCR denitration - Google Patents
The device and method of catalyst sections on-line regeneration in SCR denitration Download PDFInfo
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- CN109966919A CN109966919A CN201910268879.0A CN201910268879A CN109966919A CN 109966919 A CN109966919 A CN 109966919A CN 201910268879 A CN201910268879 A CN 201910268879A CN 109966919 A CN109966919 A CN 109966919A
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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
- 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
- B01D53/8696—Controlling the catalytic process
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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
- B01D53/88—Handling or mounting catalysts
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- 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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- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention discloses a kind of device and method of catalyst sections on-line regeneration in SCR denitration, smoke-intake pipe and pipe are separately connected at the top and bottom of SCR reactor, the multiple flue gases arranged side by side of setting are in charge of in the SCR reactor, each flue gas is in charge of equal to be connected to the smoke-intake pipe, one end of the pipe connection smoke backflow pipe, the heat exchanger for heating flue gas is connected in the smoke backflow pipe, the other end of the smoke backflow pipe is connected to hot-blast main, the hot-blast main sequentially passes through multiple flue gases arranged side by side and is in charge of, each flue gas is in charge of at least one hot blast manifold of accommodating, the SCR reactor is separated into multiple logical cigarette district domains corresponding with the hot blast manifold position by vertical baffle, multiple catalyst layers are parallel and horizontal subdivision is arranged in the logical cigarette district domain, the SCR The device and method of catalyst sections on-line regeneration are successively regenerated and are cleaned to the logical cigarette district domain of each of catalyst layer in denitration, improve the service life of catalyst layer.
Description
Technical field
The present invention relates to catalyst wash technical field of regeneration in SCR denitration, in particular in a kind of SCR denitration
The device and method of catalyst sections on-line regeneration.
Background technique
With the rapid development of our country's economy, the pollution level of atmosphere is also increasingly sharpened.In China, dust emission control and
Flue gas desulfurization technique has also reached its maturity, and gathers dust and flue gas desulfurization project is carrying out in an orderly manner, however to national ring
Guaranteed request is increasingly stringenter, and the control standard of nitrogen oxides will be gradually stringent, and existing cement kiln SNCR denitration technology can not
Meet the requirement of current environmental emission standard.And the NO of cement kilnxThe processing of emission reduction SCR denitration just starts to start to walk, therefore, right
The research of the SCR denitration work of cement kiln is of great significance to air contaminant treatment.
Currently, the flue-gas temperature condition stub that SCR denitration is applicable according to catalyst, can incite somebody to action generally according to different temperature
SCR technique is divided into: high temperature, medium temperature, middle low temperature, four kinds of low temperature different SCR techniques.High temperature SCR is generally referred to as catalyst
Applicable temperature is at 450-600 DEG C or more, and Medium temperature SCR refers to the Applicable temperature of catalyst at 320-450 DEG C, and middle low-temperature SCR is
The Applicable temperature of finger catalyst is at 180-300 DEG C, and low-temperature SCR refers to the Applicable temperature of catalyst at 80-150 DEG C.Work at present
In industry using it is wide be middle temperature catalyst that running temperature is in 320-450 DEG C, cement production enterprise Medium temperature SCR is arranged in
Behind the outlet kiln tail preheater C1 before waste heat boiler, but dust concentration is up to 80~100g/Nm3, easily cause catalyst pores to block,
Abrasion, poisoning are unable to run, and low temperature SCR denitration is arranged in after the blower of tail portion, and temperature is at 180-220 DEG C, dust 20-50
g/Nm3.This temperature range meets the temperature condition of low temperature catalyst, but due in low temperature SCR denitration reaction process, due to cigarette
There are SO in gas2、SO3Hydrogen sulfate ammonia is generated after spraying ammonia, hydrogen sulfate ammonia is a kind of extremely sticky goods and materials, is adhered to catalyst
Surface, and will continue to adherency fly ash granule, cause SCR catalyst dust stratification to block, hydrogen sulfate ammonia is a kind of powdery goods and materials of dry state,
When generating more, it will increase flying dust concentration in flue gas, aggravate the abrasion of catalyst.Just because of above-mentioned reason cement production enterprise
SCR denitration is gone no further.
SO3With the NH in flue gas3Reaction equation is as follows:
NH3+ SO3+ H2O→NH4HSO4
The reaction equation reversible reaction, when temperature is higher than 350 DEG C, which is inversely carried out, so if a kind of skill can be invented
Art inhibits the generation of hydrogen sulfate ammonia or makes hydrogen sulfate ammonolysis craft, is able to maintain catalyst and is in high efficiency state, improves catalyst
Service life will be the Gospel of cement production enterprise.
Summary of the invention
The present invention is directed to solve above-mentioned technical problem to a certain extent.
In view of this, the present invention provides a kind of device and method of catalyst sections on-line regeneration in SCR denitration, it should
In SCR denitration the device and method of catalyst sections on-line regeneration to each of catalyst layer lead to cigarette district domain successively carry out regeneration and
Cleaning, improves the service life of catalyst layer.
In order to solve the above-mentioned technical problems, the present invention provides a kind of dresses of catalyst sections on-line regeneration in SCR denitration
It sets and method, smoke-intake pipe and pipe is separately connected at the top and bottom of SCR reactor, setting is multiple in the SCR reactor
Flue gas arranged side by side is in charge of, each flue gas be in charge of it is equal be connected to the smoke-intake pipe, pipe connection smoke backflow pipe
One end, the heat exchanger for heating flue gas is connected in the smoke backflow pipe, and the other end of the smoke backflow pipe is connected to heat
Wind general pipeline, the hot-blast main sequentially pass through multiple flue gases arranged side by side and are in charge of, and each flue gas is in charge of at least accommodating one
A hot blast manifold, the SCR reactor are separated into multiple logical cigarette districts corresponding with the hot blast manifold position by vertical baffle
Domain, multiple catalyst layers are parallel and horizontal subdivision is arranged in the logical cigarette district domain.
Further, each logical cigarette district domain is equipped with soot blower.
Further, each catalyst layer is equipped with preparing catalyst layer, and the preparing catalyst layer is arranged described
The lower section of catalyst layer.
Further, the smoke backflow pipe is also connected with blower and bag filter, the bag filter, the blower
It is set gradually with the heat exchanger along the direction that the smoke backflow inner tube smoke flows.
Further, the rear of the blower is arranged in the SCR reactor.
Further, the flue gas is in charge of, the hot-blast main and the hot blast manifold are equipped with electric gate valve, described electronic
Gate valve is controlled by remote controllers.
A kind of method of catalyst sections on-line regeneration in SCR denitration, it is de- based on any SCR of claims 1 to 6
The device of catalyst sections on-line regeneration in nitre,
S1: flue gas enters in SCR reactor, the NH in SCR reactor3Catalyst layer carries out denitration to flue gas, generates simultaneously
NH4HSO4；
S2: SCR reactor is discharged in the flue gas after denitration, and the flue gas after a small amount of discharge is dusted, and the flue gas after dedusting is heated
Heating；
S3: by the NH in SCR reactor4HSO4It is divided into multiple logical cigarette district domains, the flue gas after heating is successively to multiple logical cigarette district domains
NH4HSO4It is decomposed, while keeping not carrying out NH4HSO4The logical cigarette district domain decomposed carries out denitration.
Further, the temperature in the S2 after flue gas heating is more than or equal to 350 °.
Further, to NH in the S13Catalyst layer carries out soot blowing.
The technical effects of the invention are that: (1) pipe be connected to one end of smoke backflow pipe, is connected in smoke backflow pipe
For heating the heat exchanger of flue gas, the other end of smoke backflow pipe is connected to hot-blast main, and each flue gas, which is in charge of, at least accommodates one
Hot blast manifold, SCR reactor is separated into multiple logical cigarette district domains corresponding with hot blast manifold position by vertical baffle, multiple to urge
Agent layer is parallel and horizontal subdivision is arranged in logical cigarette district domain, and flue gas recirculation uses, reduce energy consumption, reduce investment and operation at
This.
(2) blower is arranged at the outlet return pipeline of SCR reactor, avoids carrying out the flue gas of denitration not yet through overheating
Wind branch pipe enters in hot-blast main.
(3) flue gas is in charge of, hot-blast main and hot blast manifold are equipped with electric gate valve, and electric gate valve passes through remote controllers control
System controls electric gate valve by remote controllers, successively makes the NH in each logical cigarette district domain4HSO4It is decomposed, while keeping other
NH is not carried out4HSO4Decompose logical cigarette district domain carry out denitration, to catalyst layer each of lead to cigarette district domain successively carry out regeneration and clearly
It washes, improves the service life of catalyst layer.
Detailed description of the invention
Fig. 1 is that the structure of the device and method of catalyst sections on-line regeneration in a kind of SCR denitration according to the present invention is shown
It is intended to.
Wherein, 1- leads to cigarette district domain；2- catalyst layer；3-SCR reactor；4- smoke-intake pipe；5- pipe；6- smoke backflow
Pipe；7- heat exchanger；8- hot-blast main；9- partition；10- electric gate valve；11- preparing catalyst layer；12- blower；13- bag-type dust
Device；41- flue gas is in charge of；81- hot blast manifold.
Specific embodiment
The present invention will be further explained below with reference to the attached drawings and specific examples, so that those skilled in the art can be with
It better understands the present invention and can be practiced, but illustrated embodiment is not as a limitation of the invention.
As shown in Figure 1, in a kind of SCR denitration catalyst sections on-line regeneration device, the top and bottom of SCR reactor 3
Portion is separately connected smoke-intake pipe 4 and pipe 5, and the multiple flue gases arranged side by side of setting are in charge of 41 in SCR reactor 3, and each flue gas is in charge of
41 are connected to smoke-intake pipe 4, and pipe 5 is connected to one end of smoke backflow pipe 6, are connected in smoke backflow pipe 6 for heating cigarette
The other end of the heat exchanger 7 of gas, smoke backflow pipe 6 is connected to hot-blast main 8, and hot-blast main 8 sequentially passes through multiple flue gases arranged side by side
It is in charge of 41, each flue gas is in charge of 41 and at least accommodates a hot blast manifold 81, and SCR reactor 3 is separated into multiple by vertical baffle 9
Logical cigarette district domain 1 corresponding with 81 position of hot blast manifold, multiple catalyst layers 2 are parallel and horizontal subdivision is arranged in logical cigarette district domain 1,
Flue gas is in charge of 41, hot-blast main 8 and hot blast manifold 81 is equipped with electric gate valve 10, and electric gate valve 10 passes through remote controllers control
System.
According to a particular embodiment of the invention, in a kind of SCR denitration catalyst sections on-line regeneration device, SCR reaction
The top of device 3 connects smoke-intake pipe 4, and the multiple flue gases arranged side by side of setting are in charge of 41 in SCR reactor 3, each flue gas be in charge of 41 with
Smoke-intake pipe 4 is connected to, the multiple catalyst layers 2 of setting in SCR reactor 3, and the bottom of SCR reactor 3 connects pipe 5, flue gas from
Smoke-intake pipe 4 enters, and is in charge of 41 by multiple flue gases arranged side by side and enters in SCR reactor 3, catalyst in flue gas and SCR reactor 3
NH in layer 23Reaction carries out denitration, while generating NH4HSO4It is attached to catalyst layer 2, the neat stress after denitration is from pipe 5
Discharge.
Pipe 5 is connected to one end of smoke backflow pipe 6, and the heat exchange for heating neat stress is connected in smoke backflow pipe 6
The other end of device 7, smoke backflow pipe 6 is connected to hot-blast main 8, and hot-blast main 8 sequentially passes through multiple flue gases arranged side by side and is in charge of 41, often
A flue gas is in charge of 41 and at least accommodates a hot blast manifold 81, and part neat stress is passed through return pipe 6, and the heat exchanger 7 in return pipe 6 is right
Neat stress is heated, and the neat stress after heating is passed through in hot-blast main 8, then enters SCR reactor 3 from hot blast manifold 81
In, make the NH of catalyst layer 24HSO4Temperature increase, and then to NH4HSO4It is decomposed, uses flue gas recirculation, reduce energy
Consumption reduces investment and operating cost.
SCR reactor 3 is separated into multiple logical cigarette district domains 1 corresponding with 81 position of hot blast manifold by vertical baffle 9, multiple
Catalyst layer 2 is parallel and horizontal subdivision is arranged in logical cigarette district domain 1, and flue gas is in charge of 41, hot-blast main 8 and hot blast manifold 81 is all provided with
There is electric gate valve 10, electric gate valve 10 is controlled by remote controllers, is controlled electric gate valve 10 by remote controllers, is successively made
The NH in each logical cigarette district domain 14HSO4It is decomposed, while other being kept not carry out NH4HSO4The logical cigarette district domain 1 decomposed is taken off
Nitre is successively regenerated and is cleaned to logical cigarette district domain 1, and the service life of catalyst layer 2 is improved.
As shown in Figure 1, each logical cigarette district domain 1 is equipped with soot blower.
According to a particular embodiment of the invention, soot blower blows away the dust on 2 surface of catalyst layer, is keeping denitration reaction just
Often operation.
As shown in Figure 1, the lower section of multiple catalyst layers 2 is additionally provided with multiple preparing catalyst layers 11, multiple preparing catalysts
Layer 11 is parallel and horizontal subdivision is arranged.
According to a particular embodiment of the invention, when catalyst layer 2 is stopped using because of failure and other reasons, start spare catalysis
Oxidant layer 11 keeps the reaction in SCR reactor 3 to operate normally.
As shown in Figure 1, smoke backflow pipe 6 is also connected with blower 12 and bag filter 13, bag filter 13, blower 12
The direction of flow of flue gas is set gradually along smoke backflow pipe 6 with heat exchanger 7.
According to a particular embodiment of the invention, neat stress successively passes through bag filter 13, blower 12 and heat exchanger 7, only
Flue gas by blower 12 enter smoke backflow pipe 6 in, make neat stress flowing provide power, bag filter 13 to neat stress into
Row dedusting avoids high concentrate dust from entering in SCR reactor 3, causes secondary blocking to catalyst layer 2.
As shown in Figure 1, the rear of blower 12 is arranged in SCR reactor 3.
According to a particular embodiment of the invention, so that flue gas in SCR reactor 3 is in barotropic state always, avoid not yet
The flue gas for carrying out denitration enters in hot-blast main 8 by hot blast manifold 81, ensure that the normal operation of equipment.
As shown in Figure 1, in a kind of SCR denitration catalyst sections on-line regeneration method, based on claims 1 to 6 it is any
SCR denitration in catalyst sections on-line regeneration device,
S1: flue gas enters in SCR reactor 3, the NH in SCR reactor 33Catalyst layer 2 carries out denitration to flue gas, produces simultaneously
Raw NH4HSO4；
S2: SCR reactor 3 is discharged in the flue gas after denitration, and the flue gas after a small amount of discharge is dusted, and the flue gas after dedusting is heated
Heating；
S3: by the NH in SCR reactor 34HSO4It is divided into multiple logical cigarette district domains 1, the flue gas after heating is successively to multiple logical cigarette districts
The NH in domain 14HSO4It is decomposed, while keeping not carrying out NH4HSO4The logical cigarette district domain 1 decomposed carries out denitration.
According to a particular embodiment of the invention, flue gas enters in SCR reactor 3, the NH in SCR reactor 33Catalyst
2 pairs of flue gas of layer carry out denitration, while NH3With the SO in flue gas3And H2O generates NH4HSO4。
SCR reactor 3 is discharged in flue gas after denitration, and the flue gas after a small amount of discharge is dusted, and the flue gas after dedusting is added
Heat is warming up to 350 °.
By the NH in SCR reactor 34HSO4It is divided into multiple logical cigarette district domains 1, the flue gas after heating is successively to multiple logical cigarette districts
The NH in domain 14HSO4It is decomposed, by NH4HSO4The NH generated after decomposition3、SO3And H2O is discharged in SCR reactor 3, keeps simultaneously
NH is not carried out4HSO4The logical cigarette district domain 1 decomposed carries out denitration.
According to a particular embodiment of the invention, to NH in S13Catalyst layer 2 carries out soot blowing, guarantees the normal operation of reaction.
Embodiment described above is only to absolutely prove preferred embodiment that is of the invention and being lifted, protection model of the invention
It encloses without being limited thereto.Those skilled in the art's made equivalent substitute or transformation on the basis of the present invention, in the present invention
Protection scope within.Protection scope of the present invention is subject to claims.
Claims (9)
1. the device of catalyst sections on-line regeneration in a kind of SCR denitration, be separately connected at the top and bottom of SCR reactor into
Smoke pipe and pipe, which is characterized in that the multiple flue gases arranged side by side of setting are in charge of in the SCR reactor, each flue gas point
The connection of smoke-intake pipe described in Guan Junyu, one end of the pipe connection smoke backflow pipe, the interior connection of the smoke backflow pipe are useful
It is connected to hot-blast main in the other end of the heat exchanger of heating flue gas, the smoke backflow pipe, the hot-blast main sequentially passes through more
A flue gas arranged side by side is in charge of, and each flue gas is in charge of at least one hot blast manifold of accommodating, the SCR reactor and passes through perpendicular
Multiple logical cigarette district domains corresponding with the hot blast manifold position are separated into partition, multiple catalyst layers are parallel and level is divided
Every setting in the logical cigarette district domain.
2. the device of catalyst sections on-line regeneration in SCR denitration according to claim 1, which is characterized in that Mei Gesuo
It states logical cigarette district domain and is equipped with soot blower.
3. the device of catalyst sections on-line regeneration in SCR denitration according to claim 1, which is characterized in that Mei Gesuo
It states catalyst layer and is equipped with preparing catalyst layer, the lower section of the catalyst layer is arranged in the preparing catalyst layer.
4. the device of catalyst sections on-line regeneration in SCR denitration according to claim 1, which is characterized in that the cigarette
Gas return pipe is also connected with blower and bag filter, and the bag filter, the blower and the heat exchanger are along the cigarette
The direction of flow of flue gas is set gradually in gas return pipe.
5. the device of catalyst sections on-line regeneration in SCR denitration according to claim 4, which is characterized in that the SCR
The rear of the blower is arranged in reactor.
6. the device of catalyst sections on-line regeneration in SCR denitration according to claim 1, which is characterized in that the cigarette
Gas is in charge of, the hot-blast main and the hot blast manifold are equipped with electric gate valve, and the electric gate valve passes through remote controllers control
System.
7. a kind of method of catalyst sections on-line regeneration in SCR denitration, based on any SCR denitration of claims 1 to 6
The device of middle catalyst sections on-line regeneration, which is characterized in that
S1: flue gas enters in SCR reactor, the NH in SCR reactor3Catalyst layer carries out denitration to flue gas, generates simultaneously
NH4HSO4；
S2: SCR reactor is discharged in the flue gas after denitration, and the flue gas after a small amount of discharge is dusted, and the flue gas after dedusting is heated
Heating；
S3: by the NH in SCR reactor4HSO4It is divided into multiple logical cigarette district domains, the flue gas after heating is successively to multiple logical cigarette district domains
NH4HSO4It is decomposed, while keeping not carrying out NH4HSO4The logical cigarette district domain decomposed carries out denitration.
8. the method for catalyst sections on-line regeneration in SCR denitration according to claim 7, which is characterized in that the S2
Temperature after middle flue gas heating is more than or equal to 350 °.
9. the method for catalyst sections on-line regeneration in SCR denitration according to claim 7, which is characterized in that the S1
In to NH3Catalyst layer carries out soot blowing.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201910268879.0A CN109966919A (en) | 2019-04-04 | 2019-04-04 | The device and method of catalyst sections on-line regeneration in SCR denitration |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201910268879.0A CN109966919A (en) | 2019-04-04 | 2019-04-04 | The device and method of catalyst sections on-line regeneration in SCR denitration |
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ID=67082879
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111151130A (en) * | 2020-02-27 | 2020-05-15 | 东方电气集团东方锅炉股份有限公司 | SCR (selective catalytic reduction) flue gas denitration system with online regeneration function for garbage incinerator and denitration method thereof |
| CN114653202A (en) * | 2022-03-31 | 2022-06-24 | 成都达奇环境科技有限公司 | Catalytic flue gas desulfurization tower |
| CN114950128A (en) * | 2022-03-31 | 2022-08-30 | 成都达奇环境科技有限公司 | Catalytic flue gas desulfurization tower |
| CN114950127A (en) * | 2022-03-31 | 2022-08-30 | 成都达奇环境科技有限公司 | Catalytic flue gas desulfurization tower |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111151130A (en) * | 2020-02-27 | 2020-05-15 | 东方电气集团东方锅炉股份有限公司 | SCR (selective catalytic reduction) flue gas denitration system with online regeneration function for garbage incinerator and denitration method thereof |
| CN114653202A (en) * | 2022-03-31 | 2022-06-24 | 成都达奇环境科技有限公司 | Catalytic flue gas desulfurization tower |
| CN114950128A (en) * | 2022-03-31 | 2022-08-30 | 成都达奇环境科技有限公司 | Catalytic flue gas desulfurization tower |
| CN114950127A (en) * | 2022-03-31 | 2022-08-30 | 成都达奇环境科技有限公司 | Catalytic flue gas desulfurization tower |
| CN115282767A (en) * | 2022-03-31 | 2022-11-04 | 成都达奇环境科技有限公司 | Catalytic flue gas desulfurization tower |
| CN114950128B (en) * | 2022-03-31 | 2024-04-19 | 成都达奇科技股份有限公司 | Catalytic flue gas desulfurization tower |
| CN114950127B (en) * | 2022-03-31 | 2024-05-03 | 成都达奇科技股份有限公司 | Catalytic flue gas desulfurization tower |
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| Date | Code | Title | Description |
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| PB01 | Publication | ||
| PB01 | Publication | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20190705 |