CN108310972B - Multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration and application thereof - Google Patents

Multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration and application thereof Download PDF

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CN108310972B
CN108310972B CN201810233296.XA CN201810233296A CN108310972B CN 108310972 B CN108310972 B CN 108310972B CN 201810233296 A CN201810233296 A CN 201810233296A CN 108310972 B CN108310972 B CN 108310972B
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flue gas
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scr
reaction zone
bin
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CN108310972A (en
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徐瑞年
周向
张传波
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MCC Capital Engineering and Research Incorporation Ltd
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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
    • B01D53/90—Injecting reactants
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon 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
    • B01D53/8621—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
    • B01D53/8668—Removing organic compounds not provided for in B01D53/8603 - B01D53/8665
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/708—Volatile organic compounds V.O.C.'s
    • 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
    • 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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  • Environmental & Geological Engineering (AREA)
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  • General Chemical & Material Sciences (AREA)
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Abstract

The invention provides a multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration and application thereof, which sequentially comprises a flue gas main inlet, a reactor main body and a flue gas main outlet according to the flow direction of flue gas; the reactor main body is internally provided with at least one reaction unit, each reaction unit comprises a first reaction bin and a second reaction bin, the first reaction bin is serially connected with the second reaction bin and is used for containing a CO oxidation reaction catalyst, the second reaction bin is used for containing an SCR reaction catalyst, the first reaction bin is provided with a flue gas inlet communicated with a flue gas main inlet, the second reaction bin is provided with a flue gas outlet communicated with the flue gas main outlet, the first reaction bin and the second reaction bin are arranged side by side and are separated by a first heat conduction plate, and the first reaction bin and the second reaction bin are mutually communicated to form a first flue gas reaction channel allowing flue gas to pass through. The invention utilizes the heat-conducting plate to transfer the heat released by CO oxidation reaction to the SCR reaction area, thereby improving the energy utilization rate and reducing the operation cost of reheating the flue gas.

Description

Multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration and application thereof
Technical Field
The invention relates to a multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration, and belongs to the field of environmental protection.
Background
In the metallurgical industry, a large number of high-temperature combustion processes are often involved, resulting in the production of a large amount of Nitrogen Oxides (NO) x ) In the fields of chemical production, oil and gas refining and coal-fired power generation, the NO-rich gas can be generated x The flue gas of (2). The denitration treatment means that the generated NO is treated x Reduction to N 2 Thereby removing NO in the smoke x The mainstream process in the world is divided into: SCR and SNCR.
The Selective Catalytic Reduction (SCR) denitration technology is the most widely applied flue gas denitration technology internationally at present, is basically applied to most power plants in national regions such as Japan, europe, america and the like, has no byproducts, does not form secondary pollution, has a simple device structure, and has the advantages of high removal efficiency (up to more than 90 percent), reliable operation, convenience in maintenance and the like.
The SCR technical principle is as follows: under the action of catalyst, ammonia is sprayed into the fume at a certain temp. to make NO produce x Reduction to N 2 And H 2 And O. However, the current SCR catalyst mainly aims at the denitration working condition of NO under the medium-high temperature condition (220 ℃ -420 ℃), and x the method comprises the steps of removing, wherein the temperature of flue gas which is generated in the actual metallurgical production process and needs denitration is relatively low, for example, sintering flue gas is generally about 120 ℃, coking flue gas is about 200 ℃, in addition, the flue gas can enter an SCR reactor after dust removal, desulfurization and other processes are carried out, the temperature of the flue gas is usually lower than the temperature of needed denitration reaction, heating equipment is needed to heat the flue gas and then send the flue gas into the SCR reactor, the flue gas needs to be heated by consuming fuel gas in the reheating process, the general steel industry can select blast furnace gas or mixed gas of the blast furnace gas and coke oven gas to burn and preheat the flue gas, the technical scheme is generally adopted, certain operation cost is generated by using a heating furnace, in addition, a plurality of domestic steel industry desulfurization and denitration projects belong to post-modification projects, the size of the hot blast furnace is small due to site limitation, the burning heating area is short, the gas is not fully burnt, unburned CO gas with a certain content can enter the flue gas, on one hand, the flue gas emission problem can be caused when the content of the hot blast furnace is too high, on the other hand, the flue gas emission of the hot blast furnace can be influenced, and other pollutants can not reach the standard. More significant is that the emission requirements of CO emission are not made in the industries of ferrous metallurgy, chemical production and the like at present, but clear CO emission requirements are made in the waste incineration industry, and it is believed that with the continuous enhancement of environmental protection treatment strength, the relevant regulations of CO emission are also likely to be made in the ferrous metallurgy process with higher CO emission level.
Disclosure of Invention
In order to meet the environmental requirements, one of the purposes of the invention is to provide a multifunctional catalytic reactor coupling CO catalytic oxidation and SCR denitration, which can enable the CO catalytic oxidation and the SCR denitration to organically cooperate with each other, meanwhile, the reactor can be suitable for the actual production working condition, and the reaction heat can be effectively utilized.
Another object of the present invention is to provide the use of the above multifunctional catalytic reactor.
In order to achieve the aim, the invention provides a multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration, which sequentially comprises a flue gas main inlet, a reactor main body and a flue gas main outlet according to the flow direction of flue gas;
the reactor main body internally comprises at least one reaction unit, each reaction unit comprises a first reaction bin and a second reaction bin, the first reaction bin is used for containing a CO oxidation reaction catalyst and the second reaction bin is used for containing an SCR reaction catalyst, the first reaction bin is provided with a flue gas inlet communicated with the flue gas main inlet, the second reaction bin is provided with a flue gas outlet communicated with the flue gas main outlet, the first reaction bin and the second reaction bin are arranged side by side and are separated by a first heat conduction plate, and the first reaction bin and the second reaction bin are communicated with each other to form a first flue gas reaction channel allowing flue gas to pass through.
The multifunctional catalytic reactor coupled with CO catalytic oxidation and SCR denitration as described above, wherein the second reaction chamber is divided into a first SCR reaction zone, a second SCR reaction zone and a third SCR reaction zone which are sequentially communicated by a transverse plate and a longitudinal plate which are arranged at the middle lower part thereof, the longitudinal plate is a second heat conducting plate, the first SCR reaction zone and the third SCR reaction zone are arranged side by side and separated by the second heat conducting plate, the second SCR reaction zone is located above the first SCR reaction zone and the third SCR reaction zone, the first SCR reaction zone is communicated with the bottom of the first reaction chamber by a diversion bend, the bottom of the second SCR reaction zone is respectively communicated with the first SCR reaction zone and the third SCR reaction zone, and the top end of the second SCR reaction zone is open towards the flue gas inlet;
a smoke inlet of the first reaction bin is provided with a first movable baffle door capable of swinging, and the smoke inlet of the first reaction bin and the top end of the second SCR reaction zone are opened and closed alternately through the reciprocating swinging of the first movable baffle door; a second swing baffle door capable of swinging is arranged in the diversion bent pipe, and the diversion bent pipe is opened and closed through the reciprocating swing of the second swing baffle door;
when the first movable baffle door closes the flue gas inlet of the first reaction bin and opens the top end of the second SCR reaction zone, and the second movable baffle door closes the diversion elbow, the flue gas main inlet, the second SCR reaction zone, the third SCR reaction zone and the flue gas main outlet are communicated in sequence to form a second flue gas reaction channel allowing flue gas to pass through.
The multifunctional catalytic reactor coupling the CO catalytic oxidation and the SCR denitration is characterized in that two ends of the first movable baffle door are respectively a first connecting end and a first swinging end, the first connecting end can be rotatably connected with the upper end of the first heat conducting plate, and the first swinging end can be covered on the top end of the second SCR reaction area or on the flue gas inlet of the first reaction bin; the two ends of the second movable baffle door are respectively provided with a second connecting end and a second swinging end, the second connecting end is rotatably connected with the inner wall of the diversion elbow, and the second swinging end can be lapped at the lower end of the second heat conducting plate or plugged on the diversion elbow.
The multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration is characterized in that more than two reaction units are arranged side by side, and the first movable baffle door of each reaction unit can be mutually overlapped with the first movable baffle of the adjacent reaction unit and covers the top end of the corresponding second SCR reaction zone or the flue gas inlet of the first reaction bin.
The multifunctional catalytic reactor coupling CO catalytic oxidation and SCR denitration is characterized in that the first swing end and the second swing end are both provided with flexible sealing strips.
The multifunctional catalytic reactor coupled with the CO catalytic oxidation and the SCR denitration is characterized in that the flexible sealing strip is an all-stainless steel flexible sealing strip, a fluoroether rubber flexible sealing strip, a flexible sealing strip, fluororubber or polytetrafluoroethylene flexible sealing strip.
The multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration is characterized in that a guide plate and/or a finishing grid are/is arranged at the total inlet of the flue gas.
The multifunctional catalytic reactor coupling CO catalytic oxidation and SCR denitration as described above, wherein the first and second thermally conductive plates are low carbon steel thermally conductive plates, low alloy steel thermally conductive plates, or metal-plated enamel thermally conductive plates.
On the other hand, the invention provides the application of the multifunctional catalytic reactor coupling CO catalytic oxidation and SCR denitration in purifying flue gas through medium-high temperature SCR reaction.
Preferably, the flue gas is a sintering flue gas or a coking flue gas containing or not containing CO. More preferably, the CO and NO are contained x The sintering flue gas or the coking flue gas is generated by preheating the flue gas by using blast furnace gas or mixed gas of the blast furnace gas and coke oven gas.
In conclusion, the invention has the following beneficial technical effects:
1. according to the invention, the CO oxidation and SCR denitration reaction are integrated into one reactor in a partition series connection mode, the relative sizes of the CO oxidation reaction zone and the SCR denitration reaction zone can be adjusted according to the requirements of actual working conditions, and the reactor is modularly designed and convenient to adjust and implement.
2. The invention has the advantages that the CO reaction and the SCR denitration reaction are connected in series, the heat released by CO oxidation can be utilized to heat the flue gas, the SCR reaction is facilitated, and the heat released by CO oxidation can be transferred to the SCR reaction zone by utilizing the heat conducting plate by adopting the separated arrangement of the two reaction zones, so that the energy utilization rate is improved, and the operation cost of flue gas reheating is reduced.
3. The CO oxidation reaction zone can be short-circuited by the design of the movable baffle door, the arrangement can adapt to different working conditions in production, when the temperature of the flue gas of the upstream process reaches the temperature required by SCR reaction, the hot blast stove does not work, the CO oxidation reaction zone is not needed at the moment, the CO reaction zone can be closed by adjusting the baffle door, CO oxidation catalysts are saved, and the service life is prolonged.
4. The invention also has the development potential of simultaneously treating multiple pollutants, the first SCR reaction zone and the third SCR reaction zone can also be set as catalytic desorption zones aiming at other pollutants, such as catalytic oxidation zones of organic matters such as VOCs, dioxin and the like, the temperature interval of the catalytic reaction of the pollutants is similar to that of the SCR denitration reaction, and the catalytic oxidation zones can be arranged before and after the SCR process according to the process requirements.
Drawings
FIG. 1 is an internal perspective view of a preferred configuration of a multi-functional catalytic reactor for coupling CO catalytic oxidation and SCR denitration as used in an embodiment of the present invention.
Fig. 2 is a top view of the interior of the multi-functional catalytic reactor of fig. 1.
FIG. 3 is an internal perspective view of the multi-functional catalytic reactor of FIG. 1 when the CO catalytic oxidation zone is short-circuited.
The numbers in the figures have the following meanings:
1-a flue gas main inlet; 2-a reactor body; 3-a total smoke outlet; 4-a reaction unit; 5-a first reaction bin; 6-a second reaction bin; 61-a first SCR reaction zone; 62-a second SCR reaction zone; 63-a third SCR reaction zone; 7-a first thermally conductive plate; 8-a second thermally conductive plate; 9-diversion bend pipe; 10-a flexible sealing strip; 11-a first movable flapper door; 111-a first connection end; 112-a first swing end; 12-a second movable flapper door; 121-a second connection end; 122-second swing end; 13-a deflector; and 14-arranging the grids.
Detailed Description
For a more clear understanding of the technical features, objects and advantages of the present invention, reference is now made to the following detailed description taken in conjunction with the accompanying specific embodiments, and the technical solutions of the present invention are described, it being understood that these examples are intended to illustrate the present invention and are not intended to limit the scope of the present invention. In the examples, each raw reagent material is commercially available, and the experimental method not specifying the specific conditions is a conventional method and a conventional condition well known in the art, or a condition recommended by an instrument manufacturer.
In the present invention, the CO oxidation reaction catalyst is an existing catalyst, and may be a metal oxide type catalyst consisting of a single metal or oxides of a plurality of metals.
The SCR reaction catalyst is the existing catalyst, the working temperature is 250 ℃ to 400 ℃, the catalyst can be a vanadium-titanium catalyst, and important active components are vanadium pentoxide and titanium oxide.
SCR in the present invention refers to selective catalytic reduction (selective catalytic reduction) of NO using a catalyst and a reductant x The smoke is reduced and purified.
The CO catalytic oxidation of the invention refers to the generation of nontoxic CO by using a catalyst to perform catalytic oxidation reaction on toxic gas CO and oxygen at a lower temperature 2 The process of (1).
The internal perspective view of the multifunctional catalytic reactor coupling CO catalytic oxidation and SCR denitration selected in the following embodiment of the invention is shown in FIG. 1, and the state shown in FIG. 1 is suitable for the working condition requiring the use of a CO oxidation reaction zone (when the upstream process flue gas temperature cannot reach the temperature required by SCR reaction, a hot blast stove needs to work). The internal plan view of fig. 1 is shown in fig. 2. FIG. 3 is an internal perspective view of the multi-functional catalytic reactor of FIG. 1 when the CO catalytic oxidation zone is short-circuited, the condition shown in FIG. 3 being suitable for conditions where the CO oxidation reaction zone is not needed (when the upstream process flue gas temperature has reached the temperature required for the SCR reaction, the hot blast stove is not needed).
As shown in fig. 1 to fig. 3, the multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration used in the following embodiments sequentially includes a flue gas inlet 1, a reactor main body 2, and a flue gas outlet 3 in a flow direction of flue gas from upstream to downstream; the reactor main body 2 includes three repeated reaction units 4 arranged in parallel, and the number of the reaction units 4 may be one, two or more as required, which is not limited in the present invention. Each reaction unit 4 (outlined by a dotted line in fig. 1) is serially connected with a first reaction bin 5 including a CO catalytic oxidation zone for placing a CO oxidation reaction catalyst and a second reaction bin 6 including an SCR reaction zone for placing an SCR reaction catalyst, the upper end of the first reaction bin 5 is provided with a flue gas inlet, the lower end of the first reaction bin is provided with a flue gas outlet, the upper end and the lower end of the second reaction bin 6 can be used for allowing flue gas to enter and exit, the first reaction bin 5 and the second reaction bin 6 are arranged side by side and separated by a first heat conduction plate 7, the first heat conduction plate 7 is used for transferring heat generated by the CO catalytic oxidation zone to the SCR reaction zone, and the first reaction bin 5 and the second reaction bin 6 are mutually communicated to form a first flue gas reaction channel allowing flue gas to pass through.
As shown in fig. 1, the second reaction chamber 6 is divided into a first SCR reaction zone 61, a second SCR reaction zone 62 and a third SCR reaction zone 63 which are communicated in sequence by a transverse plate and a longitudinal plate arranged at the lower part thereof, the longitudinal plate is a second heat conduction plate 8, the first SCR reaction zone 61 and the third SCR reaction zone 63 are arranged side by side and separated by the second heat conduction plate 8, the second SCR reaction zone 62 is located above the first SCR reaction zone 61 and the third SCR reaction zone 63, the first SCR reaction zone 61 is communicated with the bottom of the first reaction chamber 5 by a diversion elbow 9 to guide flue gas from the first reaction chamber 5 into the first SCR reaction zone 61, and the diversion elbow 9 is formed by extending and bending from the lower part of the outer side wall of the chamber body of the first reaction chamber 5 and connected with the second heat conduction plate 8. The bottom of the second SCR reaction zone 62 is respectively communicated with the first SCR reaction zone 61 and the third SCR reaction zone 63, so that the flue gas can sequentially flow through the first reaction chamber 5, the first SCR reaction zone 61, the second SCR reaction zone 62 and the third SCR reaction zone 63, and is discharged from the flue gas main outlet 3. The top end of the second SCR reaction zone 62 is open towards the general flue gas inlet, so that when the first flue gas reaction channel is closed, flue gas can enter from the second SCR reaction zone 62, and the effect of short-circuiting the CO catalytic oxidation zone is achieved, which is described in detail below.
A first movable baffle door 11 capable of swinging is arranged at a flue gas inlet of the first reaction chamber 5, two ends of the first movable baffle door 11 are respectively a first connecting end 111 and a first swinging end 112, the first connecting end 111 is hinged or pivoted with the first heat conducting plate 7, so that the first movable baffle door 11 can swing back and forth by taking the first connecting end 111 as an axis, the first movable baffle door 11 is just covered on the top end of the second SCR reaction zone 62 (including but not limited to the condition of overlapping with the first movable baffles of the adjacent reaction units) or covered on the flue gas inlet of the first reaction chamber 5 (including but not limited to the condition of overlapping on the inner wall of the reactor main body 2 and overlapping with the first movable baffles of the adjacent reaction units) when being at two ends of swinging, so that the flue gas inlet of the first reaction chamber 7 and the top air inlet of the second SCR reaction zone 62 are opened and closed alternately by the back and forth swinging of the first movable baffle door 11, so as to control the flue gas to enter or not enter the first reaction chamber 5. Therefore, the effect of alternately switching on and off the first flue gas reaction channel and the second flue gas reaction channel is realized. As shown in fig. 1, in the present embodiment, the first flapper door 11 overlaps with the first flapper of the adjacent reaction unit and covers the top end of the corresponding second SCR reaction zone.
A second swing baffle door 12 capable of swinging is arranged in the diversion elbow 9, two ends of the second swing baffle door 12 are respectively a second connecting end 121 and a second swing end 122, the second connecting end 121 is rotatably connected with the inner wall of the diversion elbow 9, and the second swing end 122 can be lapped at the lower end of the second heat conducting plate 8 or plugged on the inner wall of the diversion elbow 9, so that the diversion elbow 9 is opened and closed through the reciprocating swing of the second swing baffle door 12 to seal the first reaction chamber 5 and control the flue gas to enter or not enter the first SCR reaction zone 61.
Under the combined action of the first movable baffle door 11 and the second movable baffle door 12, when the first movable baffle door 11 closes the flue gas inlet of the first reaction bin 5 and opens the top end of the second SCR reaction zone 62, and the second movable baffle door 12 closes the diversion elbow 9, the flue gas main inlet 1, the second SCR reaction zone 62, the third SCR reaction zone 63 and the flue gas main outlet 3 are sequentially communicated to form a second flue gas reaction channel allowing flue gas to pass through, so as to achieve the effect of short-circuiting the CO catalytic oxidation zone.
As shown in fig. 1 and 3, a deflector 13 and a finishing grid 14 are installed in the flue gas inlet 1, so that the flue gas can uniformly enter the CO catalytic oxidation zone (first reaction chamber 5) when CO catalytic oxidation reaction is required or enter the SCR reaction zone (second reaction chamber 6) when CO catalytic oxidation reaction is not required.
Further, flexible seal tape 10 is mounted on both first swing end 112 of first movable-flapper door 11 and second swing end 122 of second movable-flapper door 12. By adopting the method, the leakage of the flue gas between different reaction zones can be reduced. The flexible sealing strip is an existing product, and in some embodiments, the flexible sealing strip 10 is an all-stainless steel flexible sealing strip, a fluoroether rubber flexible sealing strip, a fluororubber flexible sealing strip or a polytetrafluoroethylene flexible sealing strip. Preferably a flexible bead of polytetrafluoroethylene.
Further, the first heat conducting plate 7 and the second heat conducting plate 8 are low carbon steel heat conducting plates, low alloy steel heat conducting plates or metal-plated enamel heat conducting plates. Metal-plated enamel heat-conducting plates are preferred.
When the multifunctional catalytic reactor is used:
the state shown in fig. 1 is applicable to the following examples 1 and 2 (when the temperature of the flue gas in the upstream process cannot reach the temperature required by the SCR reaction, the hot blast stove needs to work), two by two first movable baffle doors 11 installed on the first heat conducting plate 7 in the reactor main body 2 are overlapped with each other, so that the flue gas firstly enters the CO catalytic oxidation zone, but not firstly enters the SCR reaction zone, and a second movable baffle door 12 installed at the end of the diversion elbow 9 is overlapped with the bottom end of the second heat conducting plate 8, so that the flue gas after the reaction in the CO reaction zone enters the first SCR reaction zone 61, then passes through the second SCR reaction zone 62 and the third SCR reaction zone 63 in sequence, and the flue gas discharged from the third SCR reaction zone 63 is merged and then discharged from the flue gas main outlet 3.
The conditions shown in fig. 3 apply to the following example 3 (where the upstream process flue gas temperature can reach the temperature required for the SCR reaction and the hot blast stove need not be operated) for conditions where the CO oxidation reaction zone is not required, which can be obtained from the conditions shown in fig. 1, and the reactor for this condition can be obtained by changing the orientation of the first movable baffle door 11 provided on the first heat conducting plate 7 and the orientation of the second movable baffle door 12 at the end of the flow-guiding elbow 9.
Specifically, in fig. 3, the first movable baffle door 11 on the first heat-conducting plate 7 located at the leftmost side in the reactor is overlapped on the inner wall of the reactor to seal the CO catalytic oxidation zone at the leftmost side, the second first heat-conducting plate and the first movable baffle door 11 of the third first heat-conducting plate are overlapped with each other to open the left SCR reaction zone and seal the middle CO catalytic oxidation zone, and the fourth first heat-conducting plate and the first movable baffle door 11 of the fifth first heat-conducting plate are overlapped with each other to open the middle and right SCR reaction zones and seal the right CO catalytic oxidation zone; and the second movable baffle doors 12 arranged on the respective return bends of the left side reaction unit, the middle reaction unit and the right reaction unit are respectively lapped on the first heat conducting plate 7 suspended in the diversion elbow 9, the bottom end of each second movable baffle door seals the CO catalytic oxidation zone and opens the SCR zone, at the moment, the first flue gas channel in the reactor is sealed, the second flue gas channel is conducted, all the CO catalytic oxidation zones are in short circuit, the flue gas cannot enter the zone, the flue gas directly enters the SCR reaction zone and is discharged from the zone after reaction.
Example 1
Under a certain working condition, the temperature of the flue gas is between 170 ℃ before entering the hot blast stove, the temperature of the flue gas is between 230 ℃ after passing through the hot blast stove, the CO content in the flue gas is between 6500ppm and NO x Is-300 mg/Nm 3 The smoke amount is 110000Nm 3 H is used as the reference value. This example used a multi-functional catalytic reactor in the state shown in FIG. 1, having 3 repeating reaction units therein.
In the reactor in the state, the CO catalytic oxidation zone is in a working state, and a flexible polytetrafluoroethylene sealing strip is arranged at the movable end of the baffle door so as to reduce the leakage of flue gas between different reaction zones;
introducing flue gas to pass through the CO catalytic oxidation zone 211, wherein the CO catalytic oxidation zone 211, the third SCR reaction zone 2123 and the first heat-conducting plate between the first SCR reaction zone and the second SCR reaction zone are made of enamel-coated carbon steel, the temperature of the flue gas after passing through the CO catalytic oxidation zone 211 is increased to 245 ℃, the flue gas continuously enters the SCR reaction zone 212, namely sequentially passes through the first SCR reaction zone 2121, the third SCR reaction zone 2123 and the second SCR reaction zone 2122, and then the denitration process is completed, wherein the CO content in the flue gas is reduced to be below 100ppm, and the NO is reduced to be below 100ppm x The content can be reduced to 50mg/Nm 3 The following.
Example 2
Under another working condition, the temperature of the flue gas is 170 ℃ before entering the hot blast stove, 290 ℃ after passing through the hot blast stove, the CO content in the flue gas is 3200ppm x Is-300 mg/Nm 3 The smoke amount is 110000Nm 3 H is used as the reference value. This example used a multi-functional catalytic reactor in the state shown in FIG. 1, having 3 repeating reaction units therein.
In the reactor in the state, the CO catalytic oxidation zone is in a working state, and the movable end of the baffle door is provided with the fluororubber flexible sealing strip so as to reduce the leakage of flue gas between different reaction zones;
introducing flue gas to pass through the CO catalytic oxidation zone, wherein the first heat-conducting plate between the CO catalytic oxidation zone and the second SCR reaction zone and the first SCR reaction zone, and the second heat-conducting plate between the first SCR reaction zone and the second SCR reaction zone are made of low alloy steel, the flue gas temperature rises to 245 ℃ after passing through the CO catalytic oxidation zone, the flue gas continuously enters the SCR reaction zone, namely sequentially passes through the first SCR reaction zone, the second SCR reaction zone and the third SCR reaction zone, the denitration process is completed, the CO content in the flue gas is reduced to below 100ppm, and the NOx content can be reduced to 15mg/Nm 3 The following.
Example 3
Under another working condition, the temperature of the flue gas is 250 ℃ before the flue gas enters the hot blast stove, the requirement of the working temperature of the denitration catalyst is met, the CO content in the flue gas is 1000ppm x Is-800 mg/Nm 3 The smoke amount is 220000Nm 3 H is used as the reference value. This example used a multi-functional catalytic reactor in the state shown in fig. 3, which had 3 repeating reaction units therein.
In the reactor in the state, the CO catalytic oxidation area is in a short circuit state, and the movable end of the baffle door is provided with the fluoroether rubber sealing strip, so that the leakage of flue gas among different catalyst bins is reduced;
introducing flue gas to pass through the SCR reaction, selecting low-carbon steel as a first heat conducting plate between the CO catalytic oxidation zone and the third SCR reaction zone as well as between the CO catalytic oxidation zone and the first SCR reaction zone, and selecting low-carbon steel as a second heat conducting plate between the first SCR reaction zone and the second SCR reaction zone to finish the denitration process, wherein NO is generated x The content can be reduced to 150mg/Nm 3 The following.
In the invention, the technical problems that a large amount of CO which is not fully combusted is generated in the process of using the hot blast stove to reheat flue gas in the steel industry and SCR denitration is needed are considered, CO catalytic oxidation and SCR denitration reaction are coupled and integrated in one reactor, and the CO oxidation and SCR denitration reaction are integrated in one reactor in a partition series connection mode. In addition, the mode that CO catalytic oxidation area and SCR denitration reaction area are arranged side by side and heat-conducting plates are connected in series through bending back and used is adopted, so that heat emitted by CO oxidation can heat flue gas, SCR reaction is facilitated, the energy utilization rate is improved, and the operation cost of flue gas reheating is reduced.
The movable baffle door can short circuit the CO oxidation reaction zone, the arrangement can adapt to different working conditions in production, when the temperature of the flue gas in the upstream process reaches the temperature required by SCR reaction, the hot blast stove does not work, at the moment, the CO oxidation reaction zone does not need to be used, the CO reaction zone can be closed by adjusting the baffle door, and the service life of the CO oxidation catalyst is saved.
In addition, the first SCR reaction zone or the third SCR reaction zone is replaced by a VOCs catalytic oxidation zone or a dioxin catalytic oxidation zone. VOCs oxidation catalysts are filled in the VOCs catalytic oxidation area, the catalysts are existing catalysts, dioxin oxidation catalysts are filled in the dioxin catalytic oxidation area, and the catalysts are existing catalysts. Because the temperature range of the catalytic reaction of the pollutants is close to the SCR denitration reaction, the pollutants can be arranged before and after the SCR process according to the process requirements.
On the other hand, the invention provides the application of the multifunctional catalytic reactor coupling CO catalytic oxidation and SCR denitration in purifying flue gas through medium-high temperature SCR reaction.
Preferably, the flue gas is a sintering flue gas or a coking flue gas containing or not containing CO. More preferably, the CO and NO are contained x The sintering flue gas or the coking flue gas is generated by preheating the flue gas by using blast furnace gas or mixed gas of the blast furnace gas and coke oven gas.
Finally, the following is explained: although the present invention has been described in detail with reference to the above embodiments, it should be understood by those skilled in the art that: modifications and equivalents may be made thereto without departing from the spirit and scope of the invention and it is intended to cover any modifications or equivalents as may fall within the scope of the invention.

Claims (7)

1. A multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration sequentially comprises a flue gas main inlet, a reactor main body and a flue gas main outlet according to the flow direction of flue gas;
the reactor main body internally comprises at least one reaction unit, each reaction unit comprises a first reaction bin and a second reaction bin, the first reaction bin is used for containing a CO oxidation reaction catalyst and the second reaction bin is used for containing an SCR reaction catalyst, the first reaction bin is provided with a flue gas inlet which can be communicated with the flue gas main inlet, the second reaction bin is provided with a flue gas outlet which is communicated with the flue gas main outlet, the first reaction bin and the second reaction bin are arranged side by side and are separated by a first heat conduction plate, and the first reaction bin and the second reaction bin are communicated with each other to form a first flue gas reaction channel for allowing flue gas to pass through;
the second reaction bin is divided into a first SCR reaction zone, a second SCR reaction zone and a third SCR reaction zone which are sequentially communicated through a transverse plate and a longitudinal plate which are arranged at the middle lower part of the second reaction bin, the longitudinal plate is a second heat conduction plate, the first SCR reaction zone and the third SCR reaction zone are arranged side by side and are separated by the second heat conduction plate, the second SCR reaction zone is positioned above the first SCR reaction zone and the third SCR reaction zone, the first SCR reaction zone is communicated with the bottom of the first reaction bin through a diversion elbow, the bottom of the second SCR reaction zone is respectively communicated with the first SCR reaction zone and the third SCR reaction zone, and the top end of the second SCR reaction zone is opened towards the direction of the total flue gas inlet;
a smoke inlet of the first reaction bin is provided with a first movable baffle door capable of swinging, and the smoke inlet of the first reaction bin and the top end of the second SCR reaction zone are opened and closed alternately through the reciprocating swinging of the first movable baffle door; a second swing baffle door capable of swinging is arranged in the diversion bent pipe, and the diversion bent pipe is opened and closed through the reciprocating swing of the second swing baffle door;
when the first movable baffle door closes the flue gas inlet of the first reaction bin and opens the top end of the second SCR reaction zone, and the second movable baffle door closes the diversion elbow, the flue gas main inlet, the second SCR reaction zone, the third SCR reaction zone and the flue gas main outlet are communicated in sequence to form a second flue gas reaction channel allowing flue gas to pass through;
the two ends of the first movable baffle door are respectively a first connecting end and a first swinging end, the first connecting end can be rotatably connected with the upper end of the first heat conducting plate, and the first swinging end can be covered on the top end of the second SCR reaction area or on the flue gas inlet of the first reaction bin; the two ends of the second movable baffle door are respectively a second connecting end and a second swinging end, the second connecting end is rotatably connected with the inner wall of the diversion elbow, and the second swinging end can be lapped at the lower end of the second heat conducting plate or plugged on the diversion elbow;
the reaction units are arranged side by side, and the first movable baffle door of each reaction unit can be mutually lapped with the first movable baffle of the adjacent reaction unit and covers the top end of the corresponding second SCR reaction zone or the flue gas inlet of the first reaction bin.
2. The CO catalytic oxidation and SCR denitration coupled multifunctional catalytic reactor of claim 1, wherein a flexible sealing strip is mounted on each of the first swing end and the second swing end.
3. The multifunctional catalytic reactor for CO catalytic oxidation and SCR denitration coupling of claim 2, wherein the flexible sealing strip is an all-stainless steel flexible sealing strip, a fluoroether rubber flexible sealing strip, a fluororubber or polytetrafluoroethylene flexible sealing strip.
4. The multifunctional catalytic reactor coupling CO catalytic oxidation and SCR denitration of any one of claims 1 to 3, characterized in that a flow guide plate and/or a finishing grid is installed at the flue gas main inlet.
5. The CO catalytic oxidation and SCR denitration coupled multifunctional catalytic reactor of any one of claims 1-3, wherein said first and second thermally conductive plates are low carbon steel thermally conductive plates, low alloy steel thermally conductive plates or metal-plated enamel thermally conductive plates.
6. Use of a multifunctional catalytic reactor according to any of claims 1 to 5 for the purification of flue gas by medium-high temperature SCR reaction.
7. The use according to claim 6, wherein the flue gas is a sintering flue gas or a coking flue gas containing or not containing CO;
the sintering flue gas or the coking flue gas containing CO is generated by preheating flue gas by using blast furnace gas or mixed gas of the blast furnace gas and coke oven gas.
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