CN109603528B - Denitration system of multistage reaction device and working method thereof - Google Patents
Denitration system of multistage reaction device and working method thereof Download PDFInfo
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- CN109603528B CN109603528B CN201811650908.1A CN201811650908A CN109603528B CN 109603528 B CN109603528 B CN 109603528B CN 201811650908 A CN201811650908 A CN 201811650908A CN 109603528 B CN109603528 B CN 109603528B
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- 238000003541 multi-stage reaction Methods 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title claims abstract description 15
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 266
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 128
- 238000005507 spraying Methods 0.000 claims abstract description 100
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000003546 flue gas Substances 0.000 claims abstract description 51
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 37
- 239000000428 dust Substances 0.000 claims abstract description 27
- 239000000779 smoke Substances 0.000 claims abstract description 17
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 11
- 238000006243 chemical reaction Methods 0.000 claims description 20
- 239000003054 catalyst Substances 0.000 claims description 9
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000006477 desulfuration reaction Methods 0.000 claims description 7
- 230000023556 desulfurization Effects 0.000 claims description 7
- 230000005611 electricity Effects 0.000 claims description 5
- 230000001276 controlling effect Effects 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 2
- 238000002347 injection Methods 0.000 description 7
- 239000007924 injection Substances 0.000 description 7
- 239000007789 gas Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
Classifications
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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
-
- 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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to a denitration system of a multistage reaction device and a working method thereof, wherein the denitration system comprises a boiler, an economizer ash bucket, a baffle door adjusting device, an ammonia spraying mixing device, a reducing agent supply system, a denitration reactor, an air preheater, a dust removing device, a desulfurizing device, a plasma denitration device and a chimney; the flue gas enters the economizer after being discharged from the boiler, ash is removed through an ash bucket of the economizer, the flue gas passes through a first-stage baffle door adjusting device, a second-stage baffle door adjusting device, a first-stage ammonia spraying mixing device and a second-stage ammonia spraying mixing device, then enters a first-stage denitration reactor and a second-stage denitration reactor, then sequentially enters an air preheater, a dust removing device, a desulfurizing device, a third-stage baffle door adjusting device, a fourth-stage baffle door adjusting device and a plasma denitration device, and finally is discharged into a chimney. The invention has simple system flow, flexible operation and high denitration efficiency, and can solve the problem that NO is caused by NO operation due to denitration caused by low smoke temperature of low unit load x And the problems of risk of exceeding emission and the like, and has wide application prospect.
Description
Technical Field
The invention relates to a denitration system of a multistage reaction device and a working method thereof, belonging to the field of industrial waste gas purification, environmental protection and energy.
Background
The SCR flue gas denitration technology is adopted by most of coal-fired power plant denitration projects in China due to the advantages of stability, high efficiency and the like, and the general denitration efficiency can reach more than 80%. Only increasing the ammonia spraying amount to improve the denitration efficiency often causes ammonium bisulfate generation along with exceeding ammonia escape, and has great harm to the safe and stable operation of a denitration device and downstream equipment, and the difficulty of actual control of the uniformity of a refined flow field required by high denitration efficiency is high. Meanwhile, in view of the severe situations of short operation time, low load and the like commonly faced by the current coal-fired power plant, the coal-fired power plant is expected to be kept in a low-load operation situation in the future for a long time, so that denitration cannot be put into operation or denitration efficiency cannot be kept up due to low-smoke temperature of load brought by the situation, finally, environmental protection exceeding risk is greatly improved, and operation stability and reliability of a denitration device are affected.
In the prior art, CN105771646a discloses a double-chamber reactor for SCR denitration, which solves the problem of insufficient vertical space of a denitration plate by realizing parallel arrangement through common wall plate connection between two denitration reactors, but because only one-stage ammonia injection grid is used, the required refined flow field uniformity of high denitration efficiency cannot be achieved, and the bottom of the reactor is easier to deposit ash, in addition, the reactor is arranged, when a unit is operated, the double-chamber reactor must be operated synchronously, and when the unit is operated under low load, the risk that a denitration device cannot be put into operation due to low smoke temperature cannot be avoided.
In the prior art, CN107694305A discloses an SCR denitration system with two stages of reactors connected in series and a working method thereof, and NO can be realized by arranging the two stages of reactors in series in an inverted U shape and arranging a first-stage ammonia spraying mixing device in front of each stage of reactors x The problem of the common deposition abrasion of traditional SCR denitration technique is got rid of to the high efficiency, but because only adjust the second grade reactor flow field through setting up the guide plate between the two-stage tandem reactor, and this kind of arrangement often two-stage reactor links to each other the flue is shorter, can't fully optimize the second grade reactor flow field, and this kind of reactor tandem arrangement in addition, must two-stage reactor synchronous operation when the unit operates and when the unit low-load operation, because of the low risk that leads to the denitration device to put into operation of cigarette temperature also can't be avoided.
Disclosure of Invention
The invention aims to overcome the defects in the prior art, and provides the high-efficiency and reliable high-efficiency and high-reliability coal-fired power plant flue gas NO x A denitration system of a multistage reaction device with high denitration efficiency and low load operation, which is required by ultra-low emission and even lower emission, and a working method thereof.
The invention solves the problems by adopting the following technical scheme: a multi-stage reaction device's denitration system, its characterized in that: the device comprises a boiler, an economizer ash bucket, a first-stage baffle door adjusting device, a first-stage ammonia spraying mixing device, a second-stage baffle door adjusting device, a second-stage ammonia spraying mixing device, a reducing agent supply system, a first-stage denitration reactor, a second-stage denitration reactor, an air preheater, a dust removing device, a desulfurizing device, a third-stage baffle door adjusting device, a fourth-stage baffle door adjusting device, a plasma denitration device and a chimney; the boiler is communicated with the economizer, an economizer ash bucket is arranged below the economizer, the economizer is respectively communicated with the primary denitration reactor and the secondary denitration reactor, a primary baffle door adjusting device and a primary ammonia spraying mixing device are arranged between the economizer and the primary denitration reactor, a secondary baffle door adjusting device and a secondary ammonia spraying mixing device are arranged between the economizer and the secondary denitration reactor, a reducing agent supply system is respectively connected with the primary ammonia spraying mixing device and the secondary ammonia spraying mixing device, the primary denitration reactor and the secondary denitration reactor are both communicated with the air preheater, the dust removing device and the desulfurizing device are sequentially communicated, one path of the desulfurizing device is directly connected with the chimney, the four-stage baffle door adjusting device is arranged between the outlet of the desulfurizing device and the inlet of the chimney, the other path of the desulfurizing device is communicated with the chimney through the plasma denitration device, and the three-stage baffle door adjusting device is arranged between the outlet of the desulfurizing device and the inlet of the plasma denitration device.
The primary denitration reactor and the secondary denitration reactor are arranged in parallel.
The first-stage baffle door adjusting device is arranged at the inlet of the first-stage ammonia spraying mixing device, and the second-stage baffle door adjusting device is arranged at the inlet of the second-stage ammonia spraying mixing device.
The primary ammonia spraying and mixing device is arranged at the inlet of the primary denitration reactor, and the secondary ammonia spraying and mixing device is arranged at the inlet of the secondary denitration reactor.
The size of the primary denitration reactor is designed according to the 100% design smoke volume, and the size of the secondary denitration reactor is designed according to the 100% design smoke volume.
The working method of the denitration system of the multistage reaction device is characterized by comprising the following steps of: the working method comprises the following steps: after being discharged from the boiler, the flue gas firstly enters an economizer and is subjected to ash removal through an economizer ash bucket;
when the first-stage baffle door adjusting device is opened, the second-stage baffle door adjusting device is closed, the third-stage baffle door adjusting device is closed and the fourth-stage baffle door adjusting device is opened, flue gas enters the first-stage ammonia spraying mixing device through the first-stage baffle door adjusting device, enters the first-stage denitration reactor after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device in a flue, enters the air preheater after denitration reaction, and is discharged into a chimney after passing through the dust removing device, the desulfurizing device and the fourth-stage baffle door adjusting device in sequence;
when the first-stage baffle door adjusting device is opened, the second-stage baffle door adjusting device is closed, the third-stage baffle door adjusting device is opened and the fourth-stage baffle door adjusting device is closed, flue gas enters the first-stage ammonia spraying mixing device through the first-stage baffle door adjusting device, enters the first-stage denitration reactor after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device in a flue, enters the air preheater after denitration reaction, and is discharged into a chimney after passing through the dust removing device, the desulfurizing device, the third-stage baffle door adjusting device and the plasma denitration device in sequence;
when the first-stage baffle door adjusting device is closed, the second-stage baffle door adjusting device is opened, the third-stage baffle door adjusting device is closed and the fourth-stage baffle door adjusting device is opened, flue gas enters the second-stage ammonia spraying mixing device through the second-stage baffle door adjusting device, enters the second-stage denitration reactor after being mixed with ammonia sprayed by the second-stage ammonia spraying mixing device in a flue, enters the air preheater after denitration reaction, and then is discharged into a chimney after passing through the dust removing device, the desulfurizing device and the fourth-stage baffle door adjusting device in sequence;
when the first-stage baffle door adjusting device is closed, the second-stage baffle door adjusting device is opened, the third-stage baffle door adjusting device is opened and the fourth-stage baffle door adjusting device is closed, flue gas enters the second-stage ammonia spraying mixing device through the second-stage baffle door adjusting device, enters the second-stage denitration reactor after being mixed with ammonia sprayed by the second-stage ammonia spraying mixing device in a flue, enters the air preheater after denitration reaction, and then is discharged into a chimney after passing through the dust removing device, the desulfurizing device, the third-stage baffle door adjusting device and the plasma denitration device in sequence;
when the first-stage baffle door adjusting device is opened, the second-stage baffle door adjusting device is opened, the third-stage baffle door adjusting device is closed and the fourth-stage baffle door adjusting device is opened, a part of flue gas enters the first-stage ammonia spraying mixing device through the first-stage baffle door adjusting device, enters the first-stage denitration reactor after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device in a flue, and the other part of flue gas enters the second-stage ammonia spraying mixing device through the second-stage baffle door adjusting device, enters the second-stage denitration reactor after being mixed with ammonia sprayed by the second-stage ammonia spraying mixing device in the flue, and enters the air preheater after denitration reaction, and then enters a chimney after passing through the dust removing device, the desulfurizing device and the fourth-stage baffle door adjusting device in sequence;
when the first-stage baffle door adjusting device is opened, the second-stage baffle door adjusting device is opened, the third-stage baffle door adjusting device is opened and the fourth-stage baffle door adjusting device is closed, a part of flue gas enters the first-stage ammonia spraying mixing device through the first-stage baffle door adjusting device, enters the first-stage denitration reactor after being mixed with ammonia gas sprayed by the first-stage ammonia spraying mixing device in a flue, and the other part of flue gas enters the second-stage ammonia spraying mixing device through the second-stage baffle door adjusting device, enters the second-stage denitration reactor after being mixed with ammonia gas sprayed by the second-stage ammonia spraying mixing device in the flue, enters the air preheater after being subjected to denitration reaction, and then is discharged into a chimney after passing through the dust removing device, the desulfurizing device, the third-stage baffle door adjusting device and the plasma denitration device in sequence.
Wherein, ammonia of the first-stage ammonia spraying mixing device and the second-stage ammonia spraying mixing device are provided by a reducing agent supply system.
The invention monitors the load of the unit, the gas quantity at the outlet of the economizer, the gas temperature and the NO x Concentration and air preheater inlet NO x Concentration, ammonia escape concentration and desulfurization device outlet NO x Concentration, controlling opening degree of the first-stage baffle door adjusting device, the second-stage baffle door adjusting device, the third-stage baffle door adjusting device and the fourth-stage baffle door adjusting device, and adjusting NO content x The flue gas enters the first-stage denitration reactor, the second-stage denitration reactor and the plasma denitration device, the ammonia spraying amount of the first-stage ammonia spraying mixing device and the second-stage ammonia spraying mixing device and the electricity consumption of the plasma denitration device are regulated, and the denitration efficiency of the first-stage denitration reactor, the second-stage denitration reactor and the plasma denitration device is controlled.
The smoke temperature of the primary denitration catalyst in the primary denitration reactor is 320-420 ℃; the smoke temperature of the secondary denitration catalyst in the secondary denitration reactor is 250-420 ℃.
The temperature of the inlet flue gas of the plasma denitration device is 100-140 ℃; inlet NO of the plasma denitration device x The concentration application range is 50-200mg/m 3 。
Compared with the prior art, the invention has the following advantages and effects: the two-stage denitration reactors are designed and arranged side by side according to the design of the flue gas quantity of 100%, the requirements of the flue gas quantity of a boiler under various load working conditions can be met, the denitration reactor and the plasma denitration device which participate in the denitration reaction can be flexibly switched and controlled by adjusting the opening of a baffle door, the ammonia spraying quantity of an ammonia spraying mixing device and the electricity consumption of the plasma denitration device, the existing denitration efficiency can be greatly improved, and the flue gas NO of a coal-fired power plant can be met x The ultra-low emission even lower emission requirement, and when the unit load is low and the flue gas temperature is lower than the minimum ammonia spraying temperature of the denitration device, the unit load can be switched to the secondary denitration reactor, and the normal running of the denitration device is realized through the secondary denitration catalyst, so that NO is avoided x And (5) exceeding standard emission. Compared with the prior art, the invention has the advantages of simple system flow, flexible operation, strong operability, high denitration efficiency and less energy consumption,the cost is low, and the problem that NO is caused by denitration which is not put into operation due to low smoke temperature of unit load can be solved x The risk problem of out-of-standard emission and the like, and has wide application prospect.
Drawings
FIG. 1 is a schematic diagram of the working structure of a first stage denitration reactor in an embodiment of the present invention.
FIG. 2 is a schematic diagram of the working structure of a secondary denitration reactor in an embodiment of the present invention.
Fig. 3 is a schematic overall structure of an embodiment of the present invention.
In the figure: the device comprises a boiler 1, an economizer 2, an economizer ash bucket 3, a first-stage baffle door adjusting device 4, a first-stage ammonia spraying mixing device 5, a first-stage denitration reactor 6, a second-stage baffle door adjusting device 7, a second-stage ammonia spraying mixing device 8, a second-stage denitration reactor 9, a reducing agent supply system 10, an air preheater 11, a dust removing device 12, a desulfurizing device 13, a third-stage baffle door adjusting device 14, a fourth-stage baffle door adjusting device 15, a plasma denitration device 16 and a chimney 17.
Detailed Description
The present invention will be described in further detail by way of examples with reference to the accompanying drawings, which are illustrative of the present invention and not limited to the following examples.
Examples
Referring to fig. 1 to 3, the denitration system of the multistage reaction apparatus in the present embodiment includes a boiler 1, an economizer 2, an economizer hopper 3, a primary baffle gate adjusting device 4, a primary ammonia injection mixing device 5, a secondary baffle gate adjusting device 7, a secondary ammonia injection mixing device 8, a reducing agent supply system 10, a primary denitration reactor 6, a secondary denitration reactor 9, an air preheater 11, a dust removing device 12, a desulfurization device 13, a tertiary baffle gate adjusting device 14, a quaternary baffle gate adjusting device 15, a plasma denitration device 16, and a chimney 17.
The boiler 1 is communicated with the economizer 2, the economizer ash bucket 3 is arranged below the economizer 2, the economizer 2 is respectively communicated with the primary denitration reactor 6 and the secondary denitration reactor 9, a primary baffle door adjusting device 4 and a primary ammonia spraying mixing device 5 are arranged between the economizer 2 and the primary denitration reactor 6, a secondary baffle door adjusting device 7 and a secondary ammonia spraying mixing device 8 are arranged between the economizer 2 and the secondary denitration reactor 9, the reducing agent supply system 10 is respectively connected with the primary ammonia spraying mixing device 5 and the secondary ammonia spraying mixing device 8, the primary denitration reactor 6 and the secondary denitration reactor 9 are respectively communicated with the air preheater 11, the dust removing device 12 and the desulfurizing device 13 are sequentially communicated, one path of the desulfurizing device 13 is directly connected with the chimney 17, a four-stage baffle door adjusting device 15 is arranged between the outlet of the desulfurizing device 13 and the inlet of the chimney 17, the other path of the desulfurizing device 13 is communicated with the chimney 17 through the plasma denitration device 16, and the three-stage baffle door adjusting device 14 is arranged between the outlet of the desulfurizing device 13 and the inlet of the desulfurizing device 16.
In this embodiment, the primary denitration reactor 6 and the secondary denitration reactor 9 are arranged in parallel.
In this embodiment, the first-stage baffle door adjusting device 4 is disposed at the inlet of the first-stage ammonia spraying mixing device 5, and the second-stage baffle door adjusting device 7 is disposed at the inlet of the second-stage ammonia spraying mixing device 8.
In this embodiment, the primary ammonia spraying and mixing device 5 is disposed at an inlet of the primary denitration reactor 6, and the secondary ammonia spraying and mixing device 8 is disposed at an inlet of the secondary denitration reactor 9.
In this embodiment, the primary denitration reactor 6 is designed to have a size of 100% of the design smoke amount, and the secondary denitration reactor 9 is designed to have a size of 100% of the design smoke amount.
The working method of the denitration system of the multistage reaction device is as follows: after being discharged from the boiler 1, the flue gas firstly enters the economizer 2 and is subjected to ash removal through an economizer ash bucket 3;
when the first-stage baffle door adjusting device 4 is opened, the second-stage baffle door adjusting device 7 is closed, the third-stage baffle door adjusting device 14 is closed and the fourth-stage baffle door adjusting device 15 is opened, the flue gas enters the first-stage ammonia spraying mixing device 5 through the first-stage baffle door adjusting device 4, enters the first-stage denitration reactor 6 after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device 5 in a flue, enters the air preheater 11 after denitration reaction, and then sequentially passes through the dust removing device 12, the desulfurizing device 13 and the fourth-stage baffle door adjusting device 15 and is discharged into the chimney 17;
when the first-stage baffle door adjusting device 4 is opened, the second-stage baffle door adjusting device 7 is closed, the third-stage baffle door adjusting device 14 is opened and the fourth-stage baffle door adjusting device 15 is closed, flue gas enters the first-stage ammonia spraying mixing device 5 through the first-stage baffle door adjusting device 4, enters the first-stage denitration reactor 6 after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device 5 in a flue, enters the air preheater 11 after denitration reaction, and then is discharged into the chimney 17 after passing through the dust removing device 12, the desulfurizing device 13, the third-stage baffle door adjusting device 14 and the plasma denitration device 16 in sequence;
when the first-stage baffle door adjusting device 4 is closed, the second-stage baffle door adjusting device 7 is opened, the third-stage baffle door adjusting device 14 is closed and the fourth-stage baffle door adjusting device 15 is opened, the flue gas enters the second-stage ammonia spraying mixing device 8 through the second-stage baffle door adjusting device 7, enters the second-stage denitration reactor 9 after being mixed with ammonia gas sprayed by the second-stage ammonia spraying mixing device 8 in a flue, enters the air preheater 11 after denitration reaction, and then is discharged into the chimney 17 after passing through the dust removing device 12, the desulfurizing device 13 and the fourth-stage baffle door adjusting device 15 in sequence;
when the first-stage baffle door adjusting device 4 is closed, the second-stage baffle door adjusting device 7 is opened, the third-stage baffle door adjusting device 14 is opened and the fourth-stage baffle door adjusting device 15 is closed, the flue gas enters the second-stage ammonia spraying mixing device 8 through the second-stage baffle door adjusting device 7, enters the second-stage denitration reactor 9 after being mixed with ammonia gas sprayed by the second-stage ammonia spraying mixing device 8 in a flue, enters the air preheater 11 after denitration reaction, and is discharged into the chimney 17 after passing through the dust removing device 12, the desulfurizing device 13, the third-stage baffle door adjusting device 14 and the plasma denitration device 16 in sequence;
when the first-stage baffle door adjusting device 4 is opened, the second-stage baffle door adjusting device 7 is opened, the third-stage baffle door adjusting device 14 is closed and the fourth-stage baffle door adjusting device 15 is opened, a part of flue gas enters the first-stage ammonia spraying mixing device 5 through the first-stage baffle door adjusting device 4, enters the first-stage denitration reactor 6 after being mixed with ammonia gas sprayed by the first-stage ammonia spraying mixing device 5 in a flue, and enters the second-stage ammonia spraying mixing device 8 through the second-stage baffle door adjusting device 7, enters the second-stage denitration reactor 9 after being mixed with ammonia gas sprayed by the second-stage ammonia spraying mixing device 8 in the flue, enters the air preheater 11 after denitration reaction, and then enters the chimney 17 after passing through the dust removing device 12, the desulfurizing device 13 and the fourth-stage baffle door adjusting device 15 in sequence;
when the first-stage baffle door adjusting device 4 is opened, the second-stage baffle door adjusting device 7 is opened, the third-stage baffle door adjusting device 14 is opened and the fourth-stage baffle door adjusting device 15 is closed, a part of flue gas enters the first-stage ammonia spraying mixing device 5 through the first-stage baffle door adjusting device 4, enters the first-stage denitration reactor 6 after being mixed with ammonia gas sprayed by the first-stage ammonia spraying mixing device 5 in a flue, and enters the second-stage ammonia spraying mixing device 8 through the second-stage baffle door adjusting device 7, enters the second-stage denitration reactor 9 after being mixed with ammonia gas sprayed by the second-stage ammonia spraying mixing device 8 in the flue, enters the air preheater 11 after denitration reaction, and then enters the chimney 17 after passing through the dust removing device 12, the desulfurizing device 13, the third-stage baffle door adjusting device 14 and the plasma denitration device 16 in sequence.
Ammonia gas of the primary ammonia injection mixing device 5 and the secondary ammonia injection mixing device 8 are supplied by a reducing agent supply system 10.
By monitoring the load of the unit, the gas quantity and the gas temperature at the outlet of the economizer 2 and NO x Concentration and air preheater 11 inlet NO x Concentration, ammonia escape concentration and NO at outlet of desulfurization device 13 x Concentration, controlling the opening degree of the first-stage baffle door adjusting device 4, the second-stage baffle door adjusting device 7, the third-stage baffle door adjusting device 14 and the fourth-stage baffle door adjusting device 15, and adjusting the NO content x The flue gas enters the first-stage denitration reactor 6, the second-stage denitration reactor 9 and the plasma denitration device 16, the ammonia spraying amount of the first-stage ammonia spraying mixing device 5 and the second-stage ammonia spraying mixing device 8 and the electricity consumption of the plasma denitration device 16 are regulated, and the denitration efficiency of the first-stage denitration reactor 6, the second-stage denitration reactor 9 and the plasma denitration device 16 is controlled.
The smoke temperature of the first-stage denitration catalyst in the first-stage denitration reactor 6 is 320-420 ℃; the smoke temperature of the secondary denitration catalyst in the secondary denitration reactor 9 is between 250 and 420 ℃.
The temperature of the inlet flue gas of the plasma denitration device 16 is 100-140 ℃; inlet NO of plasma denitration device 16 x The concentration application range is 50-200mg/m 3 。
The type, volume and number of layers of the denitration catalyst can be determined according to flue gas conditions and performance requirements.
The two-stage denitration reactors and the plasma denitration device 16 are organically connected in parallel, are independent and cooperate, are designed to be arranged in parallel according to the flue gas volume design of 100% through the size of the two-stage denitration reactors, can meet the requirements of the flue gas volume under various load working conditions of the boiler 1, and can flexibly switch and control the denitration reactor and the plasma denitration device 16 which participate in denitration reaction through adjusting the opening of the baffle gate, the ammonia injection amount of the ammonia injection mixing device and the electricity consumption of the plasma denitration device 16, so that the existing denitration efficiency can be greatly improved, and the flue gas NO of a coal-fired power plant can be met x The ultra-low emission and even lower emission requirements are met, and when the unit load is low and the flue gas temperature is lower than the minimum ammonia spraying temperature of the denitration device 13, the unit load can be switched to the secondary denitration reactor 9, and the denitration device 13 is normally put into operation through the secondary denitration catalyst, so that NO is avoided x And (5) exceeding standard emission. Compared with the prior art, the embodiment has the advantages of simple system flow, flexible operation, strong operability, high denitration efficiency, less energy consumption and low cost, and can solve the problem that denitration cannot be put into operation and NO is caused by low smoke temperature due to low unit load x The risk problem of out-of-standard emission and the like, and has wide application prospect.
Although the present invention is described with reference to the above embodiments, it should be understood that the invention is not limited to the embodiments described above, but is capable of modification and variation without departing from the spirit and scope of the present invention.
Claims (7)
1. A multi-stage reaction device's denitration system, its characterized in that: the device comprises a boiler (1), an economizer (2), an economizer ash bucket (3), a first-stage baffle door adjusting device (4), a first-stage ammonia spraying mixing device (5), a second-stage baffle door adjusting device (7), a second-stage ammonia spraying mixing device (8), a reducing agent supply system (10), a first-stage denitration reactor (6), a second-stage denitration reactor (9), an air preheater (11), a dust removing device (12), a desulfurizing device (13), a third-stage baffle door adjusting device (14), a fourth-stage baffle door adjusting device (15), a plasma denitration device (16) and a chimney (17); the boiler (1) is communicated with the economizer (2), the economizer ash hopper (3) is arranged below the economizer (2), the economizer (2) is respectively communicated with the primary denitration reactor (6) and the secondary denitration reactor (9), a primary baffle door adjusting device (4) and a primary ammonia spraying mixing device (5) are arranged between the economizer (2) and the primary denitration reactor (6), a secondary baffle door adjusting device (7) and a secondary ammonia spraying mixing device (8) are arranged between the economizer (2) and the secondary denitration reactor (9), the reducing agent supply system (10) is respectively connected with the primary ammonia spraying mixing device (5) and the secondary ammonia spraying mixing device (8), the primary denitration reactor (6) and the secondary denitration reactor (9) are both communicated with the air preheater (11), the dust remover (12) and the desulfurizing device (13) are sequentially communicated, the desulfurizing device (13) is directly connected with a chimney (17) and is connected with a chimney (17) through a plasma channel (17) and a flue gas desulfurization device (17) and a chimney (17) is connected with a flue gas desulfurization device (13) through a flue gas desulfurization device (17) inlet (17), the three-stage baffle door adjusting device (14) is arranged between the outlet of the desulfurization device (13) and the inlet of the plasma denitration device (16); the primary denitration reactor (6) and the secondary denitration reactor (9) are arranged in parallel; the size of the primary denitration reactor (6) is designed according to the 100% design smoke volume, and the size of the secondary denitration reactor (9) is designed according to the 100% design smoke volume; the smoke temperature of the primary denitration catalyst in the primary denitration reactor (6) is 320-420 ℃; the smoke temperature of the secondary denitration catalyst in the secondary denitration reactor (9) is 250-420 ℃.
2. The denitration system of a multistage reaction apparatus according to claim 1, characterized in that: the first-stage baffle door adjusting device (4) is arranged at the inlet of the first-stage ammonia spraying mixing device (5), and the second-stage baffle door adjusting device (7) is arranged at the inlet of the second-stage ammonia spraying mixing device (8).
3. The denitration system of a multistage reaction apparatus according to claim 1, characterized in that: the primary ammonia spraying and mixing device (5) is arranged at the inlet of the primary denitration reactor (6), and the secondary ammonia spraying and mixing device (8) is arranged at the inlet of the secondary denitration reactor (9).
4. A method of operating a denitration system of a multistage reaction apparatus according to any one of claims 1 to 3, characterized in that: the working method comprises the following steps: after being discharged from the boiler (1), the flue gas firstly enters the economizer (2) and is subjected to ash removal through an economizer ash bucket (3);
when the first-stage baffle door adjusting device (4) is opened, the second-stage baffle door adjusting device (7) is closed, the third-stage baffle door adjusting device (14) is closed and the fourth-stage baffle door adjusting device (15) is opened, flue gas enters the first-stage ammonia spraying mixing device (5) through the first-stage baffle door adjusting device (4), enters the first-stage denitration reactor (6) after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device (5) in a flue, enters the air preheater (11) after denitration reaction, and then sequentially passes through the dust removing device (12), the desulfurizing device (13) and the fourth-stage baffle door adjusting device (15) and is discharged into the chimney (17);
when the first-stage baffle door adjusting device (4) is opened, the second-stage baffle door adjusting device (7) is closed, the third-stage baffle door adjusting device (14) is opened and the fourth-stage baffle door adjusting device (15) is closed, flue gas enters the first-stage ammonia spraying mixing device (5) through the first-stage baffle door adjusting device (4), enters the first-stage denitration reactor (6) after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device (5) in a flue, enters the air preheater (11) after denitration reaction, and then sequentially passes through the dust removing device (12), the desulfurizing device (13), the third-stage baffle door adjusting device (14) and the plasma denitration device (16) and is discharged into the chimney (17);
when the first-stage baffle door adjusting device (4) is closed, the second-stage baffle door adjusting device (7) is opened, the third-stage baffle door adjusting device (14) is closed and the fourth-stage baffle door adjusting device (15) is opened, flue gas enters the second-stage ammonia spraying mixing device (8) through the second-stage baffle door adjusting device (7), and enters the second-stage denitration reactor (9) after being mixed with ammonia sprayed by the second-stage ammonia spraying mixing device (8) in a flue, and the flue gas after denitration reaction enters the air preheater (11) and then sequentially passes through the dust removing device (12), the desulfurizing device (13) and the fourth-stage baffle door adjusting device (15) and is discharged into the chimney (17);
when the first-stage baffle door adjusting device (4) is closed, the second-stage baffle door adjusting device (7) is opened, the third-stage baffle door adjusting device (14) is opened and the fourth-stage baffle door adjusting device (15) is closed, flue gas enters the second-stage ammonia spraying mixing device (8) through the second-stage baffle door adjusting device (7), and enters the second-stage denitration reactor (9) after being mixed with ammonia sprayed by the second-stage ammonia spraying mixing device (8) in a flue, and the flue gas after denitration reaction enters the air preheater (11) and then sequentially passes through the dust removing device (12), the desulfurizing device (13), the third-stage baffle door adjusting device (14) and the plasma denitration device (16) and is discharged into the chimney (17);
when the first-stage baffle door adjusting device (4) is opened, the second-stage baffle door adjusting device (7) is opened, the third-stage baffle door adjusting device (14) is closed and the fourth-stage baffle door adjusting device (15) is opened, a part of flue gas enters the first-stage ammonia spraying mixing device (5) through the first-stage baffle door adjusting device (4), enters the first-stage denitration reactor (6) after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device (5) in a flue, the other part of flue gas enters the second-stage ammonia spraying mixing device (8) through the second-stage baffle door adjusting device (7), enters the second-stage denitration reactor (9) after being mixed with ammonia sprayed by the second-stage ammonia spraying mixing device (8) in the flue, enters the air preheater (11) after denitration reaction, and then enters the chimney (17) after passing through the dust removing device (12), the desulfurizing device (13) and the fourth-stage baffle door adjusting device (15) in sequence;
when the first-stage baffle door adjusting device (4) is opened, the second-stage baffle door adjusting device (7) is opened, the third-stage baffle door adjusting device (14) is opened and the fourth-stage baffle door adjusting device (15) is closed, a part of flue gas enters the first-stage ammonia spraying mixing device (5) through the first-stage baffle door adjusting device (4), enters the first-stage denitration reactor (6) after being mixed with ammonia sprayed by the first-stage ammonia spraying mixing device (5) in a flue, another part of flue gas enters the second-stage ammonia spraying mixing device (8) through the second-stage baffle door adjusting device (7), enters the second-stage denitration reactor (9) after being mixed with ammonia sprayed by the second-stage ammonia spraying mixing device (8) in the flue, enters the air preheater (11) after denitration reaction, and then sequentially passes through the dust removing device (12), the desulfurizing device (13), the third-stage baffle door adjusting device (14) and the plasma denitration device (16) and then is discharged into the chimney (17).
5. The method for operating a denitration system of a multistage reaction apparatus according to claim 4, characterized in that: ammonia gas of the primary ammonia spraying mixing device (5) and the secondary ammonia spraying mixing device (8) are provided by a reducing agent supply system (10).
6. The method for operating a denitration system of a multistage reaction apparatus according to claim 4, characterized in that: by monitoring the load of the unit, the flue gas amount at the outlet of the economizer (2), the flue gas temperature and NO x Concentration, and air preheater (11) inlet NO x Concentration, ammonia escape concentration and NO at outlet of desulfurizing device (13) x Concentration, controlling the opening degree of a first-stage baffle door regulating device (4), a second-stage baffle door regulating device (7), a third-stage baffle door regulating device (14) and a fourth-stage baffle door regulating device (15), and regulating the NO content x The proportion of flue gas entering a primary denitration reactor (6), a secondary denitration reactor (9) and a plasma denitration device (16) is adjusted, the ammonia spraying amount of the primary ammonia spraying mixing device (5) and the secondary ammonia spraying mixing device (8) and the electricity consumption of the plasma denitration device (16) are regulated, and the primary denitration reactor (6), the secondary denitration reactor (9) and the plasma denitration device are controlledDenitration efficiency of the device (16).
7. The method for operating a denitration system of a multistage reaction apparatus according to claim 6, characterized in that: the temperature of the inlet flue gas of the plasma denitration device (16) is 100-140 ℃; inlet NO of the plasma denitration device (16) x The concentration application range is 50-200mg/m 3 。
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