CN108014613A - A kind of damp dry type flue gas purifying system and method based on Carbon Materials oxidation and denitration - Google Patents
A kind of damp dry type flue gas purifying system and method based on Carbon Materials oxidation and denitration Download PDFInfo
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- CN108014613A CN108014613A CN201610946325.8A CN201610946325A CN108014613A CN 108014613 A CN108014613 A CN 108014613A CN 201610946325 A CN201610946325 A CN 201610946325A CN 108014613 A CN108014613 A CN 108014613A
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- flue gas
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- gas purifying
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- 239000003546 flue gas Substances 0.000 title claims abstract description 97
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000003575 carbonaceous material Substances 0.000 title claims abstract description 19
- 230000003647 oxidation Effects 0.000 title claims abstract description 11
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 11
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 39
- 230000023556 desulfurization Effects 0.000 claims abstract description 38
- 239000000428 dust Substances 0.000 claims abstract description 34
- 239000007789 gas Substances 0.000 claims abstract description 30
- 239000002250 absorbent Substances 0.000 claims abstract description 14
- 230000002745 absorbent Effects 0.000 claims abstract description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 21
- 239000003054 catalyst Substances 0.000 claims description 21
- 239000003795 chemical substances by application Substances 0.000 claims description 14
- 239000011575 calcium Substances 0.000 claims description 12
- 229910052799 carbon Inorganic materials 0.000 claims description 12
- 229910052791 calcium Inorganic materials 0.000 claims description 11
- 239000012190 activator Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 230000003009 desulfurizing effect Effects 0.000 claims description 9
- 230000000903 blocking effect Effects 0.000 claims description 6
- 235000019504 cigarettes Nutrition 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 3
- 239000000571 coke Substances 0.000 claims description 3
- 239000000835 fiber Substances 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 239000012716 precipitator Substances 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 2
- 238000000889 atomisation Methods 0.000 claims description 2
- 238000005303 weighing Methods 0.000 claims description 2
- 239000000779 smoke Substances 0.000 abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 5
- 238000005516 engineering process Methods 0.000 abstract description 4
- 230000008878 coupling Effects 0.000 abstract description 2
- 238000010168 coupling process Methods 0.000 abstract description 2
- 238000005859 coupling reaction Methods 0.000 abstract description 2
- 239000012467 final product Substances 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 abstract description 2
- 230000000694 effects Effects 0.000 description 12
- 238000011069 regeneration method Methods 0.000 description 8
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 7
- 239000002956 ash Substances 0.000 description 7
- 230000003197 catalytic effect Effects 0.000 description 6
- 230000008929 regeneration Effects 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000010881 fly ash Substances 0.000 description 5
- 230000008676 import Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 238000001994 activation Methods 0.000 description 3
- 239000003610 charcoal Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000002779 inactivation Effects 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- -1 flue gas Compound Chemical class 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- 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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
-
- 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
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur 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
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- 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
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/65—Catalysts not containing noble metals
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention discloses a kind of damp dry type flue gas purifying system and method based on Carbon Materials oxidation and denitration.The damp dry type flue gas purifying system based on Carbon Materials oxidation and denitration includes desulfurization reactor, dust removing units, the storage of weary absorbent are sent, activated and humidification unit and Benitration reactor；The outlet of the desulfurization reactor is connected with the dust removing units；The exhanst gas outlet of the dust removing units is connected with the Benitration reactor；The outlet of the Benitration reactor is sequentially connected air-introduced machine and chimney；The outlet of the ash dropping hopper of the dust removing units send with the weary absorbent storage, activate and humidification unit is connected.The present invention realizes denitration, desulfurization, the coupling of dedusting technology, facility compact, and floor space is small；Using semidry method, water consumption is few, and final product is solid-state, and without handling waste water, technique is simple, can be widely used in industrial smoke processing procedure.
Description
Technical field
The present invention relates to a kind of smoke eliminator and its method, and in particular to it is a kind of based on Carbon Materials oxidation and denitration half
Dry type flue gas purification system and method.
Background technology
SCR is the most gas denitrifying technology of commercial Application at present, and wherein high temperature catalyst reaction temperature requirement is at 350 DEG C
, it is necessary to be arranged in before dust-removal and desulfurizing, the high cloud of dust gas of high-sulfur has the activity and service life of catalyst very big negative for left and right
Effect.After denitration is placed on desulfurization and dedusting by low-temperature SCR technique, but reaction temperature is generally also more than 150 DEG C, and through desulfurization with
For flue-gas temperature afterwards generally below 70 DEG C, this requires also need to reheat flue gas before denitration.In addition SCR denitration method
Using NH3Make reducing agent, ammonia belongs to dangerous material, there are certain security risk in transport and storing process, in denitrification process
There are NH3The problem of escape.
The content of the invention
The object of the present invention is to provide a kind of damp dry type flue gas purifying system and method based on Carbon Materials oxidation and denitration.
Damp dry type flue gas purifying system provided by the present invention based on Carbon Materials oxidation and denitration, it includes desulphurization reaction
Device, dust removing units, the storage of weary absorbent are sent, are activated and humidification unit and Benitration reactor；
The outlet of the desulfurization reactor is connected with the dust removing units；
The exhanst gas outlet of the dust removing units is connected with the Benitration reactor；
The outlet of the Benitration reactor is sequentially connected air-introduced machine and chimney；
The outlet of the ash dropping hopper of the dust removing units send with the weary absorbent storage, activate and humidification unit is connected.
In the present invention, the weary absorbent, which refers to having, absorbs potentiality, but the absorbent for activation process of still needing.
In the damp dry type flue gas purifying system, an air preheater is also connected with before the desulfurization reactor.
In the damp dry type flue gas purifying system, the desulfurization reactor can be riser reactor.
In the damp dry type flue gas purifying system, the dust removing units include primary deduster and the refined dedusting of connection
Device；
The primary deduster is any in cyclone dust collector, gravity type deduster and louver separator；
The refined dedusting device is any in bag filter, electric precipitator and electric bag combined dust catcher.
In the damp dry type flue gas purifying system, the weary absorbent storage send, activate and humidification unit includes phase successively
Storage bin, conveying device, activator and the humidification mixer of connection；
Blocking valve is equipped between the dust removing units and the storage bin, to prevent the negative shadow collaborated to dust removing effects
Ring；
The storage bin is in back taper, its cone angle is more than 70 °, is conducive to the flowing of solid particulate matter；
The bulkhead of the storage bin is equipped with fluidizer and air bubble；
The storage bin wall is equipped with weighing device, the metering for solid particulate matter conveying capacity；
The conveying device is revolution discharge valve or screw feeder；
The activator is equipped with finer atomization nozzle or steam nozzle, and can reserve additional solid absorbent charge door；
The activator is continous way or intermittent discharge method, and 2+N activator is used if using intermittent discharging
It is arranged in parallel, the activation effect of weary absorbent is further improved by extending soak time；
In the damp dry type flue gas purifying system, the humidification mixer passes through distributing device phase with the desulfurization reactor
Connection；
The distributing device is rounded, square or dustpan-shaped.
In the damp dry type flue gas purifying system, the exit of the air-introduced machine connects a flue gas recirculation flue duct bypass,
The flue gas recirculation flue duct bypass is connected with the heat exchanger in boiler, the outlet of the heat exchanger and the denitration reaction
The regenerated flue gas entrance of device is connected；
The regenerated flue gas outlet of the Benitration reactor is connected with the entrance of the air preheater；
When the carbon base catalyst in the Benitration reactor inactivates (i.e. NO2Gas absorption saturation) after, the cigarette can be passed through
The regeneration to the carbon base catalyst is realized in the bypass of gas cycle flue：Clean flue gas is heated by the heat exchanger, is back to institute
State in Benitration reactor；The NO for making to adsorb on carbon base catalyst using the heat effect of heat smoke2Exported again by regenerated flue gas
The import of air preheater is returned to, is converged with boiler exhaust gas, agent removing is desulfurized in desulfurization reactor.
In the damp dry type flue gas purifying system, the damp dry type flue gas purifying system includes multiple in parallel described de-
Nitre reactor, when a Benitration reactor starts regeneration, can open remaining Benitration reactor, to ensure the continuous fortune of denitration
OK.
Present invention also offers a kind of flue gas purifying method, include the following steps：Utilize the damp dry type flue gas purifying
System carries out desulphurization denitration to flue gas to be clean, obtains the flue gas for meeting discharge standard.
Wherein, the purification route of flue gas to be clean is：Flue gas to be clean is anti-into the desulfurization by the air preheater
Answer in device, with the desulfurization agent in the desulfurization reactor；Then the flue gas enters from the outlet of the desulfurization reactor
Dedusting is carried out to the dust removing units；The exhanst gas outlet of the flue gas from the dust removing units enters to the Benitration reactor
It is interior, denitration is carried out under the action of the carbon base catalyst, is then reached from the denitration exhanst gas outlet discharge of the Benitration reactor
To the flue gas for meeting discharge standard.
The desulfurizing agent can be high-calcium fly ass, and to obtain the flyash containing calcium activated, boiler oil preferably uses high calcium
Coal (when sulfur content in coal amount is 0.5~1%, CaO content ＞ 10%~20% in ash content)；, can be if fuel is low calcium coal
A certain amount of CaCO is mixed in coal3、Ca(OH)2Or CaO.Also can be by Ca (OH)2Or CaO is added in circulating ash.In order to improve desulfurization
The reactivity of agent, can by water humidification cycle ash (or water humidification cycle ash+in the reactor top spray into two level be humidified water)
Mode adjust temperature and relative humidity required in desulfurization reactor.Reaction temperature is warm away from control with nearly adiabatic saturation temperature
At 5~25 DEG C.
The carbon base catalyst can be activated carbon, activated coke, active carbocoal and/or activated carbon fibre
The present invention realizes that the principle of gas cleaning is：
In Benitration reactor under the catalytic action of carbon based material, the NO of adsorptivity difference aoxidizes generation and is more easy to by charcoal in flue gas
The NO of sill absorption2, the middle NO of flue gasxRemoved by catalytic adsorption；After Carbon Materials inactivation i.e. adsorption saturation, clean hot cigarette is passed through
Gas thermal regeneration, the high NO after regeneration2Flue gas is removed back to desulfurization reactor is interior with calcium-based desulfurizing agent.
The present invention obtains following technique effect：
The present invention, as catalyst, under the conditions of existing for low temperature and oxygen, the NO in flue gas is aoxidized using carbon based material
Into the NO easily adsorbed by Carbon Materials2, so as to remove the NO in flue gasx, removal efficiency is more than 90%.After Carbon Materials adsorption saturation,
Regenerated, can be repeatedly used by the way of heat smoke heating.
Contain NO after regeneration2Flue gas enter desulfuration reaction device in calcium-based desulfurizing agent reaction removed, greatly letter
The treatment process of accessory substance after denitration is changed.Benitration reactor is arranged in after desulfurization and dedusting, greatly reduces sulfureous in flue gas
Compound and dust to the poisoning of catalyst, block, the negative effect such as wear, and denitration reaction uses fixed-bed structure form, keeps away
The mechanical wear of catalyst in moving bed denitrating technique is exempted from.
Flue-gas temperature after desulfurization can be just passed directly at 50~90 DEG C in the temperature window of NO catalysis oxidations, flue gas
Denitration reaction is carried out in Benitration reactor, without being heated again to flue gas.
The present invention realizes denitration, desulfurization, the coupling of dedusting technology, facility compact, and floor space is small；Using semidry method,
Water consumption is few, and final product is solid-state, and without handling waste water, technique is simple, can be widely used in industrial smoke processing procedure.
Brief description of the drawings
Fig. 1 is the structure diagram of damp dry type flue gas purifying system of the present invention.
Fig. 2 is the structure diagram of Benitration reactor in invention damp dry type flue gas purifying system.
Each mark is as follows in figure：
1,2 Benitration reactor, 3 desulfurization reactors, 41 primary dedusters, 42 refined dedusting devices, 5 blocking valves, 6 storage bins, 7 is defeated
Send device, 8 activators, 9 humidification mixers, 10 distributing devices, 11 air preheaters, 12 boilers, 13 heat exchangers, the circulation of 14 regenerated flue gas
Pump, 15 air-introduced machines, 16 chimneys, 17 grey storehouses, 101,102,103,104,201,202,203,204 valves, 105 catalyst charges
Mouthful, 106 catalyst discharge ports, 107 denitration gas inlets, 108 denitration exhanst gas outlets, 109 regenerated flue gas imports, 110 regeneration cigarettes
Gas exports.
Embodiment
The present invention will be further described below in conjunction with the accompanying drawings, but the invention is not limited in following embodiments.
Experimental method used in following embodiments is conventional method unless otherwise specified.
The materials, reagents and the like used in the following examples, is commercially available unless otherwise specified.
As shown in Figure 1, it is the structure diagram of damp dry type flue gas purifying system of the present invention, the removing system and 12 phase of boiler
Connection, the back-end ductwork of boiler 12 are connected with air preheater 11, and the outlet of air preheater 11 is connected with the desulfurization reactor 3 of vertical pipe type
Connect, SO in the calcium activated removing flue gas in flyash is utilized in desulfurization reactor 32、SO3Deng sour gas.Desulfurization reactor 3
Outlet be connected with dust removing units, for by remove pollutant after flue gas carry out dedusting.Wherein, dust removing units include connecting
Cyclone dust collector, gravity type deduster and hundred may be selected in the primary deduster 41 and refined dedusting device 42 connect, primary deduster 41
Any in leaf window deduster, refined dedusting device 42 may be selected to appoint in bag filter, electric precipitator and electric bag combined dust catcher
It is a kind of.The ash port of the dust removing units sent by the storage of blocking valve 5 and weary absorbent, activate and humidification unit is connected, blocking valve 5
Effect be the negative effect for preventing from collaborating to dust removing effects.Weary absorbent storage send, activate and humidification unit includes connecting successively
Storage bin 6, conveying device 7, activator 8 and the humidification mixer 9 connect, storage bin 6 is in back taper, its cone angle is more than 70 °, favorably
In the flowing of circulating ash.Section is bored in storage bin 6 and sets cinder-discharging port, and unnecessary material is sent to grey storehouse 17 through cinder-discharging port discharge, to maintain
The material balance of system.The mixer 9 that is humidified in present system is connected with desulfurization reactor 3 by distributing device 10, distributing device
Can be rounded, square or dustpan-shaped.The exhanst gas outlet of dust removing units is connected with 2 Benitration reactors 1 and 2 in parallel, in charcoal
The NO oxidations of adsorptivity difference, which generate, under the catalytic action of sill, in flue gas is more easy to by the NO of carbon based material absorption2, in flue gas
NOxRemoved by catalytic adsorption.The outlet of Benitration reactor 1 and 2 is sequentially connected air-introduced machine 15 and chimney 16, i.e., clean flue gas is through drawing
Wind turbine 15 is discharged from chimney 16.The pipeline being connected with the smoke inlet and exhanst gas outlet of Benitration reactor 1 and 2 is equipped with valve
101st, 102,103,104,201,202,203 and 204.
When the carbon base catalyst in Benitration reactor 1 and 2 inactivates (i.e. NO2Gas absorption saturation) after, can be by setting cigarette
The regeneration to carbon base catalyst is realized in the bypass of gas cycle flue：Connected in the exit of air-introduced machine 15 by the flue gas recirculation flue
Road, the flue gas recirculation flue duct bypass are connected with the heat exchanger 13 in boiler 12, the outlet of heat exchanger 13 and denitration reaction
Device 1 is connected with 2 regenerated flue gas entrance 109；The regenerated flue gas outlet 110 of Benitration reactor 1 and 2 and the entrance of air preheater 11
It is connected；Clean flue gas is heated by heat exchanger 13, is back in Benitration reactor 1 and 2, is made using the heat effect of heat smoke
The NO adsorbed on carbon base catalyst2The import of air preheater 11 is returned to by regenerated flue gas outlet 110 again, is converged with boiler exhaust gas,
Agent removing is desulfurized in desulfurization reactor 3.
The structure for the Benitration reactor that damp dry type flue gas purifying system of the present invention uses is as shown in Fig. 2, its upper part and lower part
Catalyst feeds 105 and catalyst discharge port 106 are respectively equipped with, denitration gas inlet 107 is respectively equipped with its opposing sidewalls
With denitration exhanst gas outlet 108, regenerated flue gas import 109 and regenerated flue gas outlet 110 are additionally provided with its side wall.
The flow that gas cleaning is carried out using damp dry type flue gas purifying system of the present invention is as follows：
Boiler 12 burning produce 100~200 DEG C of flue gases through air preheater 11 heat exchange after further cool down, temperature 120 DEG C with
Under flue gas enter in the desulfurization reactor 3 of vertical pipe type, remove flue gas using the calcium activated in flyash in the desulfurization reactor 3
Middle SO2、SO3Deng sour gas；The dust in primary deduster 41 and refined dedusting device 42 removing flue gas is sequentially entered afterwards；Through de-
(50~90 DEG C) of low-temperature flue gas after sulphur dedusting enters Benitration reactor 1, under the catalytic action of carbon based material, is adsorbed in flue gas
Property difference NO oxidation generation be more easy to by carbon based material adsorb NO2, the middle NOx of flue gas removed by catalytic adsorption, clean flue gas warp
Air-introduced machine is discharged from chimney.The flyash that pre-duster 41 and refined dedusting device 42 are collected enters in storage bin 6 through blocking valve 5 to be stored up
Deposit, conveying device 7 quantitatively feeds activator 8, after the material after activation enters the uniform humidification of humidification mixing arrangement 9, then through cloth
In 10 negative pressure of device suction desulfurization reactor 3, the complete desulfurizing agent of unreacted participates in reacting again, to improve the utilization of desulfurizing agent
Rate.Unnecessary flyash is discharged into grey storehouse 17 in storage bin 6.
I.e. NO after Carbon Materials inactivation in Benitration reactor 12Gas absorption saturation, closes inlet and outlet 101 He of gas fume valve
102, regenerated flue gas inlet and outlet Flue valve 103 and 104 is opened, extension flue gas is exported through circulating fan 14 from air-introduced machine 15
Into the heat exchanger 13 in boiler 12,250~450 DEG C of clean heat smoke is heated to through regenerated flue gas imported valve 103
Into the inside of Benitration reactor 1 or chuck, (i.e. heating parsing of the heat smoke to Carbon Materials can use direct contact type, also may be used
With using contactless), the NO adsorbed after heat smoke heats in Benitration reactor 1 on Carbon Materials2Returned by outlet valve 104
To 11 import of air preheater, converge with boiler exhaust gas, agent removing is desulfurized in desulfurization reactor 3.To ensure the company of denitrification apparatus
Reforwarding row, when Benitration reactor 1 starts regeneration, while opens the inlet and outlet Flue valve 201 and 201 of Benitration reactor 2.Two
And above Benitration reactor alternately enables.
The clean-up effect of present system：
Boiler exhaust gas forms：SO2Concentration is 600mg/Nm3, NOxConcentration is 400mg/Nm3, the temperature of flue gas is 120
℃.Purified through damp dry type flue gas purifying system of the present invention, wherein, desulfurizing agent is high-calcium fly ass, and carbon base catalyst is work
Property charcoal.Purified processing, SO2Removal efficiency is 92%, NOxRemoval efficiency is 90%.
Claims (10)
1. a kind of damp dry type flue gas purifying system based on Carbon Materials oxidation and denitration, it includes desulfurization reactor, dust removing units, weary
Absorbent storage is sent, is activated and humidification unit and Benitration reactor；
The outlet of the desulfurization reactor is connected with the dust removing units；
The exhanst gas outlet of the dust removing units is connected with the Benitration reactor；
The outlet of the Benitration reactor is sequentially connected air-introduced machine and chimney；
The outlet of the ash dropping hopper of the dust removing units send with the weary absorbent storage, activate and humidification unit is connected.
2. damp dry type flue gas purifying system according to claim 1, it is characterised in that：The desulfurization reactor is vertical pipe type
Reactor；
The desulfurizing agent that the desulfurization reactor uses is high-calcium fly ass.
3. damp dry type flue gas purifying system according to claim 1 or 2, it is characterised in that：The dust removing units include connecting
The primary deduster and refined dedusting device connect；
The primary deduster is any in cyclone dust collector, gravity type deduster and louver separator；
The refined dedusting device is any in bag filter, electric precipitator and electric bag combined dust catcher.
4. damp dry type flue gas purifying system according to any one of claim 1-3, it is characterised in that：The weary absorbent
Storage give, activate and humidification unit include be sequentially connected the storage bin connect, conveying device, activator and humidification mixer；
Blocking valve is equipped between the dust removing units and the storage bin；
The storage bin is in back taper, its cone angle is more than 70 °；
The bulkhead of the storage bin is equipped with fluidizer and air bubble；
The storage bin wall is equipped with weighing device；
The conveying device is revolution discharge valve or screw feeder；
The activator is equipped with finer atomization nozzle or steam nozzle；
The activator is continous way or intermittent discharge method.
5. damp dry type flue gas purifying system according to claim 4, it is characterised in that：The humidification mixer takes off with described
Reaction of Salmon-Saxl device is connected by distributing device；
The distributing device is rounded, square or dustpan-shaped.
6. the damp dry type flue gas purifying system according to any one of claim 1-5, it is characterised in that：The air-introduced machine
Exit connects a flue gas recirculation flue duct bypass, and the flue gas recirculation flue duct bypass is connected with the heat exchanger in boiler,
The outlet of the heat exchanger is connected with the regenerated flue gas entrance of the Benitration reactor；
The regenerated flue gas outlet of the Benitration reactor is connected with the entrance of the air preheater.
7. the damp dry type flue gas purifying system according to any one of claim 1-6, it is characterised in that：The half dry type cigarette
Gas cleaning system includes multiple Benitration reactors in parallel；
The carbon base catalyst that the Benitration reactor uses is activated carbon, activated coke, active carbocoal and/or activated carbon fibre.
8. a kind of flue gas purifying method, includes the following steps：Utilize any damp dry type flue gas purifying in claim 1-7
System carries out desulphurization denitration to flue gas to be clean, obtains the flue gas for meeting discharge standard.
9. flue gas purifying method according to claim 8, it is characterised in that：The purification route of flue gas to be clean is：Treat net
The flue gas of change enters in the desulfurization reactor by the air preheater, with the desulfurization agent in the desulfurization reactor；So
The flue gas enters to the dust removing units from the outlet of the desulfurization reactor and carries out dedusting afterwards；The flue gas is from the dedusting
The exhanst gas outlet of unit is entered in the Benitration reactor, and denitration, Ran Houcong are carried out under the action of the carbon base catalyst
The denitration exhanst gas outlet discharge of the Benitration reactor reaches the flue gas for meeting discharge standard.
10. flue gas purifying method according to claim 8 or claim 9, it is characterised in that：The desulfurizing agent is high-calcium fly ass；
The carbon base catalyst is activated carbon, activated coke, active carbocoal and/or activated carbon fibre.
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| CN201610946325.8A CN108014613A (en) | 2016-11-02 | 2016-11-02 | A kind of damp dry type flue gas purifying system and method based on Carbon Materials oxidation and denitration |
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