CN108905568A - A kind of circulating fluidized bed boiler flue gas desulfuration and denitrification system and its remodeling method - Google Patents
A kind of circulating fluidized bed boiler flue gas desulfuration and denitrification system and its remodeling method Download PDFInfo
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- CN108905568A CN108905568A CN201810949659.XA CN201810949659A CN108905568A CN 108905568 A CN108905568 A CN 108905568A CN 201810949659 A CN201810949659 A CN 201810949659A CN 108905568 A CN108905568 A CN 108905568A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 239000003546 flue gas Substances 0.000 title claims abstract description 59
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000007634 remodeling Methods 0.000 title claims abstract description 6
- 239000007921 spray Substances 0.000 claims abstract description 62
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 30
- 239000002250 absorbent Substances 0.000 claims abstract description 16
- 230000002745 absorbent Effects 0.000 claims abstract description 16
- 230000023556 desulfurization Effects 0.000 claims abstract description 12
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical group [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000000908 ammonium hydroxide Substances 0.000 claims abstract description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 31
- 229920000742 Cotton Polymers 0.000 claims description 23
- 239000000446 fuel Substances 0.000 claims description 22
- 239000002893 slag Substances 0.000 claims description 22
- 239000002699 waste material Substances 0.000 claims description 22
- 230000009466 transformation Effects 0.000 claims description 16
- 238000002485 combustion reaction Methods 0.000 claims description 15
- 239000002028 Biomass Substances 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 13
- 238000003780 insertion Methods 0.000 claims description 13
- 230000037431 insertion Effects 0.000 claims description 13
- 229910021529 ammonia Inorganic materials 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 12
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 10
- 239000003245 coal Substances 0.000 claims description 9
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 239000004071 soot Substances 0.000 claims description 8
- 239000003638 chemical reducing agent Substances 0.000 claims description 7
- 230000035939 shock Effects 0.000 claims description 7
- 238000009834 vaporization Methods 0.000 claims description 7
- 230000008016 vaporization Effects 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 6
- 239000012528 membrane Substances 0.000 claims description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 5
- 239000003517 fume Substances 0.000 claims description 5
- 239000000843 powder Substances 0.000 claims description 4
- 238000013459 approach Methods 0.000 claims description 3
- 239000005864 Sulphur Substances 0.000 claims description 2
- 235000019504 cigarettes Nutrition 0.000 claims description 2
- 230000003134 recirculating effect Effects 0.000 claims description 2
- 230000008901 benefit Effects 0.000 abstract description 8
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 9
- 239000000463 material Substances 0.000 description 8
- 239000002245 particle Substances 0.000 description 8
- 239000002956 ash Substances 0.000 description 7
- 239000000839 emulsion Substances 0.000 description 7
- 206010021143 Hypoxia Diseases 0.000 description 6
- 239000000428 dust Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 229910052783 alkali metal Inorganic materials 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000002631 hypothermal effect Effects 0.000 description 3
- 208000018875 hypoxemia Diseases 0.000 description 3
- 230000007954 hypoxia Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000013517 stratification Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 238000005299 abrasion Methods 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- -1 alkali metal salts Chemical class 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 101100298222 Caenorhabditis elegans pot-1 gene Proteins 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- NNHHDJVEYQHLHG-UHFFFAOYSA-N potassium silicate Chemical class [K+].[K+].[O-][Si]([O-])=O NNHHDJVEYQHLHG-UHFFFAOYSA-N 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000009420 retrofitting Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002351 wastewater 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
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
-
- 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
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- 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
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/79—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
- B01D53/74—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
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- 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
Abstract
The present invention relates to boiler technology field, specially a kind of circulating fluidized bed boiler flue gas desulfuration and denitrification system and its remodeling method.The flue gas desulfuration and denitrification system includes desulphurization system and denitrating system, the desulphurization system includes the desulfurizing tower with the outlet connection of air-introduced machine, the exit of the desulfurizing tower is provided with demister, the inlet of desulfurization spray equipment is connect by solution feed pump with absorbent hold-up tank in the desulfurizing tower, and the absorbent is ammonium hydroxide；The denitrating system includes flue gas recirculation system, SNCR denitration system and SCR denitration system.The present invention is transformed by desulphurization system, equipment desulfuration efficiency is set to be greater than 95%, denitrating technique is cooperateed with by SNCR denitration system and SCR denitration system, NOx removal is high-efficient, flexible operation, SNCR denitration efficiency about 75%, SCR denitration efficiency is up to 90%, NOx removal is high-efficient, high efficient and reliable, has good economic benefit and environmental benefit.
Description
Technical field
The present invention relates to boiler technology field, specially a kind of circulating fluidized bed boiler flue gas desulfuration and denitrification system and its change
Make method.
Background technique
Circulating fluidized bed boiler is the highest clean coal-firing device of industrialization degree, and circulating fluidized bed boiler boiler is overall
On be divided into front and the vertical shaft of tail portion two.Front vertical shaft is always to hang structure, and surrounding is made of fin panel casing, from bottom to top, according to
Secondary is air compartment, emulsion zone, a dilute-phase zone, and back-end ductwork is followed successively by high temperature superheater, low temperature superheater from top to bottom and saves coal
Device.Tail vertical well uses support construction, is connected between two vertical shafts by vertical cyclone separator, and separator lower part couples circulating ash
Transportation system, circulating ash transportation system is mainly by feed back pipe, loop back device, a few part compositions such as overflow pipe and ash cooler.
The general fuel of circulating fluidized bed boiler in the prior art is mixed coal, and boiler load is lower, under overall operating condition at the beginning of NOx
Beginning discharge value is higher, and the qualified discharge to realize NOx can only be run by full burner hearth hypoxemia（It cannot achieve ultralow）, but full burner hearth
Hypoxemia certainly will influence boiler combustion efficiency, and furnace effect is caused to reduce.Moreover, desulfuration in furnace is with denitration in the stove, there are conflicting ground
Side, including：1）Desulfurizing agent CaCO3There is catalytic action for the generation of NOx, desulfuration in furnace increases NOx generation amount；2）It is taken off in furnace
Sulphur needs oxygen-enriched environment, and denitration in the stove requires hypoxemia operation appropriate；These repugnances, which increase in desulfuration in furnace and furnace, to be taken off
The difficulty that nitre is realized jointly.
How efficient burning and low nitrogen, desulfurization realization to be effectively combined, is circulating fluidized bed boiler in the prior art
The emphasis of transformation.
Technical solution
To solve above-mentioned problems of the prior art, this patent provides a kind of circulating fluidized bed boiler flue gas desulfuration and denitrification
System, specific technical solution are as follows：
A kind of circulating fluidized bed boiler flue gas desulfuration and denitrification system, including boiler, high temperature cyclone separator, back-end ductwork, it is described
Boiler is connected by the gas approach of reversal chamber and high temperature cyclone separator, the exhaust pass and tail of the high temperature cyclone separator
The connection of portion's flue, the exhaust pass of the back-end ductwork are successively connect with deduster, air-introduced machine, the high temperature cyclone separator
Bottom is connect by refeed line with the return port on boiler, further includes desulphurization system and denitrating system, the desulphurization system includes
With the desulfurizing tower of the outlet connection of air-introduced machine, the exit of the desulfurizing tower is provided with demister, and desulfurization is sprayed in the desulfurizing tower
The inlet of shower device is connect by solution feed pump with absorbent hold-up tank, and the absorbent is ammonium hydroxide；The denitrating system includes
Flue gas recirculation system, SNCR denitration system and SCR denitration system, the flue gas recirculation system include the outlet air with air-introduced machine
The circulating fan of mouth connection, the circulating fan are connect with primary air fan entrance and secondary air fan entrance respectively by pipeline；Institute
Stating SNCR denitration system includes：It is arranged in the SNCR denitrification spray gun that is arranged on reversal chamber, high temperature cyclone separator exhaust pass
SNCR denitrification spray gun, the SNCR denitrification spray gun being arranged in the middle part of boiler setting, the SNCR denitrification spray gun being arranged on refeed line；It is described
SCR denitration system liquid includes the SCR denitration spray equipment in desulfurizing tower, and the inlet of the SCR denitration spray equipment successively leads to
Ammonia air mixer, liquid ammonia vaporization device, heat exchanger, solution feed pump and reducing agent hold-up tank is crossed to connect.
Preferably, the circulating fluidized bed boiler flue gas desulfuration and denitrification system, further includes that biomass fuel mixes burning system
System, the biomass fuel co-combustion system include the biomass fuel transportation system and coal powder conveying system of boiler two sides setting,
The biomass fuel is waste cotton slag, and the mixed-fuel burning proportion of the waste cotton slag is 10%-15%.
Preferably, during the exit of the high temperature cyclone separator is provided in the insertion high temperature cyclone separator
Heart cylinder, the exhaust pass for connecting central tube and back-end ductwork, the central tube eccentric setting.
Preferably, the depth in the central tube insertion high temperature cyclone separator is 1700m-1800mm, the high temperature
The entrance opening dimension of cyclone separator is 820mm*2400mm, central tube is in fourth quadrant deviation Membrane Separator Cylinder for CFB Boiler center 50-
100mm, central tube diameter are 1100mm-1300mm.
Preferably, being provided with two SNCR denitrification spray guns on the reversal chamber, on high temperature cyclone separator exhaust pass
4 SNCR denitrification spray guns are set, two SNCR denitrification spray guns are arranged in boiler setting middle part, two SNCR denitrations are arranged on refeed line
Spray gun.
It is followed preferably, being provided on pipeline between the circulating fan and primary air fan entrance and secondary air fan entrance
Total wind is provided on the pipeline in the distinguished and admirable meter of ring and circulated air regulating valve, the primary air fan outlet and secondary air fan exit
Flowmeter and total wind regulating valve.
Preferably, being provided with air preheater in the back-end ductwork, the primary air fan, secondary air fan pass through air
Preheater is connect with First air entrance and Secondary Air entrance respectively.
Preferably, being provided with shock wave soot blower in the back-end ductwork, two panels water-cooling screen is provided in the boiler.
The invention also discloses a kind of circulating fluidized bed boiler flue gas desulfuration and denitrification remodeling methods, including：
（1）Desulphurization system transformation：It transform the chimney for being used to discharge fume after original air-introduced machine as desulfurizing tower, the exit of desulfurizing tower is set
Demister is set, the inlet of desulfurization spray equipment is connect by solution feed pump with absorbent hold-up tank in desulfurizing tower, and absorbent is ammonia
Water；
（2）SNCR denitration system transformation：In desulfurizing tower be arranged SCR denitration spray equipment, the SCR denitration spray equipment into
Liquid mouth passes sequentially through ammonia air mixer, liquid ammonia vaporization device, heat exchanger, solution feed pump and reducing agent hold-up tank and connects；
（3）Feed system transformation：Waste cotton slag co-combustion system is set in boiler two sides, waste cotton slag co-combustion system includes feed bin and spiral
Batcher, the waste cotton slag in feed bin enter boiler by screw(-type) feeder, and waste cotton slag mixed-fuel burning proportion is 10%-15%；
（4）Increase flue gas recirculation system：Circulating fan is connected by pipeline at the air outlet of air-introduced machine, circulating fan passes through
Pipeline is connect with primary air fan entrance and secondary air fan entrance respectively, is followed according to the exhaust gas volumn of load control system flue gas recycled and again
The proportion of ring flue gas and First air, Secondary Air；
（5）Separation system transformation：Replace the central tube of the high temperature cyclone separator, the central tube insertion high-temp. vortex separation
Depth in device is 1700m-1800mm, the entrance opening dimension of the high temperature cyclone separator is 820mm*2400mm, central tube exists
Fourth quadrant deviates Membrane Separator Cylinder for CFB Boiler center 50-100mm, central tube diameter is 1100mm-1300mm；
（6）The SNCR system reform：Connection boiler and high temperature cyclone separator reversal chamber on be arranged two SNCR denitrification spray guns,
Be arranged on high temperature cyclone separator exhaust pass 4 SNCR denitrification spray guns, two SNCR denitrification spray guns of setting in the middle part of boiler setting,
Two SNCR denitrification spray guns are set on refeed line；
（7）Shock wave soot blower is set in back-end ductwork, increases the water-cooling screen of two panels Natural Circulation in boiler.
Beneficial effect
Desulphurization system transformation of the invention has the following advantages that:（1）Absorption tower is less scaling, since ammonia is lived with higher reaction
Property, and because of the chemical characteristic of ammonium sulfite solution, determining can be to avoid fouling；（2）The byproduct generated in sweetening process can
Comprehensive utilization, and system non-wastewater discharge, it is without secondary pollution, meet the theory of circular economy and the direction of environmental protection industry development,
Moreover, because the value of by-product is higher, sulfur content is higher, and byproduct of ammonium sulfate yield is bigger, also more economical；（3）Consumption
Can be low, because being not required to drop, heating in sweetening process, absorption tower resistance is small；（4）It being not required to set bypass flue, absorbent stops for seasonable,
Flue use is made in desulfurization, does not influence the normal operation of unit, boiler；（5）Efficiently, conveniently, ammonia type flue gas desulfurizing is living for desulfurizer
Property it is strong, reaction rate is fast, desulfurizing agent be clear ammonium hydroxide clear liquid, flue gas do not have to cooling can enter desulfurizing tower carry out desulfurization it is anti-
It answers, treated, and flue gas does not have to heat up and can discharge in dew point temperatures above, and desulfuration efficiency is greater than 95%, entire sulfur removal technology stream
Journey is simple, and only need to be equipped with corresponding supervisor can run；（6）Equipment investment is low, and product is by straight for ammonia company
Take back receipts centralized processing.
The present invention cooperates with denitrating technique using SNCR denitration system and SCR denitration system, and NOx removal is high-efficient, operation spirit
Living, SNCR denitration efficiency about 75%, for SCR denitration efficiency up to 90%, NOx removal is high-efficient, high efficient and reliable, has economical well
Benefit and environmental benefit.
The method that the present invention uses flue gas recirculation, flue gas recycled is led in primary wind pipe and secondary air duct,
Using hypothermia and hypoxia feature possessed by flue gas recycled, partial fume is sprayed into boiler again, controls the cigarette of flue gas recycled
The proportion of tolerance and flue gas recycled and First air, Secondary Air reduces local temperature in boiler furnace, forms local reduction gas
Atmosphere inhibits the generation of nitrogen oxides, improves clinker coking phenomenon in boiler furnace, and improve boiler grate high temperature corrosion.Flue gas
Recycling improves the flow velocity of burner hearth and heat convection area to a certain extent, is conducive to improve Cyclone efficiency, improve
Circulating ratio extends residence time of the flying dust in furnace, is conducive to fly ash refiring；Circulating ash quantity increases simultaneously, is also beneficial to control
Material layer temperature processed, flue gas recirculation reduce the bulk temperature of burner hearth, are also beneficial to reduce nitrogen oxides, and then effectively improve
The coking phenomenon of the inner of the boiler chamber slag of boiler, while fire box temperature is controlled, and improve the high temperature corrosion of the fire grate of boiler, meanwhile,
Due to reducing the production rate of nitrogen oxides, it is possible to reduce the ammonium hydroxide usage amount of SNCR has saved operating cost；In addition, following again
Ring flue gas is derived from the clean flue gas after air-introduced machine, it is possible to reduce equipment, primary wind pipe, the product of secondary air duct and cycle flue
Grey risk.
By the transformation to separation system, improve efficiency separator, furnace exit temperature be increased to 900-930 DEG C it
Between, SNCR reaction condition is optimized, the denitration efficiency of SNCR system is greatly improved, reduces the escaping of ammonia；By being transformed above, improve
The on-load ability of boiler.
Increase soot blower system, guarantees that back-end ductwork lacks dust stratification, guarantee the heat transfer effect of back-end ductwork, reduce exhaust gas temperature.
Increase the water-cooling screen heating surface of two panels Natural Circulation, on the one hand increase furnace internal heating surface, guarantees boiler load；It is another
Furnace exit temperature can be effectively reduced in aspect, prevents separation device coking.
The present invention is transformed by desulphurization system, and equipment desulfuration efficiency is made to be greater than 95%, de- by SNCR denitration system and SCR
Nitre systematic collaboration denitrating technique, NOx removal is high-efficient, flexible operation, and SNCR denitration efficiency about 75%, SCR denitration efficiency reaches
90%, NOx removal is high-efficient, high efficient and reliable, has good economic benefit and environmental benefit.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of embodiment 1；
Fig. 2 is the structural schematic diagram of embodiment 1；
Fig. 3 is SNCR denitrification spray gun insertion position figure；
Fig. 4 is the cross-sectional structure schematic diagram of high temperature cyclone separator and boiler；
In figure, 1：Boiler, 2：High temperature cyclone separator, 3：Back-end ductwork, 4：Reversal chamber, 5：Deduster, 6：Air-introduced machine, 7：Desulfurization
Tower, 8：Refeed line, 9：Circulating fan, 10：Primary air fan, 11：Secondary air fan, 12：Central tube, 13：Exhaust pass, 14：Biology
Matter fuel delivery system, 15：Coal powder conveying system, 16：High temperature superheater, 17：Low temperature superheater, 18：Economizer, 19：Air
Preheater, 20：SNCR denitrification spray gun, 21：Recirculating air flow meter, 22：Circulated air regulating valve, 23：Total airflow meter, 24：Total wind
Regulating valve, 25：Shock wave soot blower, 26：Water-cooling screen, 27：Air distribution plate, 28：First air entrance, 29：Secondary Air entrance, 30：Demisting
Device, 31：Desulfurization spray equipment, 32：Solution feed pump, 33：Absorbent hold-up tank, 34：SCR denitration spray equipment, 35：Ammonia air is mixed
Conjunction, 36：Liquid ammonia vaporization device, 37：Heat exchanger, 38：Solution feed pump, 39：Reducing agent hold-up tank.
Specific embodiment
The invention will now be further described with reference to specific embodiments, the advantages and features of the present invention will be with description and
It is apparent.But examples are merely exemplary, and it is not intended to limit the scope of the present invention in any way.Those skilled in the art answer
It should be appreciated that without departing from the spirit and scope of the invention can details to technical solution of the present invention and form repair
Change or replace, but these modifications and replacement are fallen within the protection scope of the present invention.
Embodiment 1
As shown in Figure 1, a kind of circulating fluidized bed boiler flue gas desulfuration and denitrification system, including pot 1, high temperature cyclone separator 2, tail
Portion's flue 3, the boiler 1 are connect by reversal chamber 4 with the gas approach of high temperature cyclone separator 2, the high-temp. vortex separation
The exhaust pass of device 2 is connect with back-end ductwork 3, and the exhaust pass of the back-end ductwork 3 successively connects with deduster 5, air-introduced machine 6
Connect, the bottom of the high temperature cyclone separator 2 is connect by refeed line 8 with the return port on boiler, further include desulphurization system with
Denitrating system, the desulphurization system include the exit setting of the desulfurizing tower 7 with the desulfurizing tower 7 of the outlet connection of air-introduced machine
There is demister 30, the inlet of desulfurization spray equipment 31 is connected by solution feed pump 32 and absorbent hold-up tank 33 in the desulfurizing tower
It connects, the absorbent is ammonium hydroxide.
The denitrating system includes flue gas recirculation system, SNCR denitration system and SCR denitration system, and the flue gas follows again
Loop system includes the circulating fan 9 connecting with the air outlet of air-introduced machine 6, the circulating fan 9 by pipeline respectively with First air
10 entrance of machine is connected with 11 entrance of secondary air fan.
SNCR denitrification spray gun insertion position is as shown in figure 3, the SNCR denitration system includes：It is arranged on reversal chamber 4
It is arranged in the middle part of the SNCR denitrification spray gun that is arranged in SNCR denitrification spray gun, high temperature cyclone separator exhaust pass, boiler setting
The SNCR denitrification spray gun being arranged in SNCR denitrification spray gun, refeed line 8.
The SCR denitration system liquid includes the SCR denitration spray equipment 34 in desulfurizing tower 7, the SCR denitration spray equipment
Inlet pass sequentially through ammonia air mixing 35, liquid ammonia vaporization device 36, heat exchanger 37, solution feed pump 38 and reducing agent hold-up tank 39
Connection.
The method that the present invention uses flue gas recirculation is mixed into the clean flue gas in part in First air, utilizes recycling
Hypothermia and hypoxia feature possessed by flue gas, the fluidising air velocity of emulsion zone when by guaranteeing underload improve close when underrun
The fluidization characteristic of phase region, strengthens the mixing of emulsion zone, and more pulverized coal particle is taken to dilute-phase zone, reduces emulsion zone and burns part
Volume and temperature keep the temperature in entire burner hearth more uniform；In high load capacity, partial fume is mixed into First air, is enriched
Emulsion zone temperature adjustment means reduce emulsion zone oxygen concentration, advantageously reduce the generation of NOx.Using the method for flue gas recirculation, portion
Clean flue gas is divided to be mixed into Secondary Air, the hypothermia and hypoxia feature possessed by flue gas recycled is conducive to increase Secondary Air
The wind speed of spout strengthens dilute-phase zone gas-solid, the mixing of gas gas, reduces local temperature in the burner hearth of boiler, be conducive to avoid the formation of office
Portion high-temperature region, and local reduction atmosphere is formed, to reduce NOx generation.
Feed bin is arranged in boiler two sides, two material inlets is arranged on boiler both walls emulsion zone top, waste cotton slag is from boiler two
Side enters furnace.Cotton slag mixed-fuel burning proportion 10%-15%（With coal heat ratio）, under the operating condition, in line with burning is mixed less, frequently mix the original of burning
Then, boiler improvement project amount is small, low cost, and boiler can safe and stable operation.Waste residue cotton enters screw(-type) feeder by feed bin
(2.2kW, 7m3/ h) after, boiler is sent by screw(-type) feeder.Screw(-type) feeder revolving speed is adjusted by frequency converter, is sent with control
Enter the waste cotton quantity of slag in boiler.By taking back boiler First air, waste cotton material is sent into burner hearth.Pneumatic lock gate hatch shields,
Thermocouple sensor is provided with before flashboards, when temperature is excessively high, it is believed that be tempered, close lock gate hatch in time, stop
It is fed motor.
Biomass fuel has following characteristic compared with coal：Chlorinity and alkali metal content are high, fugitive constituent is high, oxygen content is high,
Moisture content is high, fixed carbon is low, ash content is low, calorific value is low, sulfur content is low.Biomass is because potassium, chlorinity are higher, so ash after burning
In contain a large amount of alkali metal salts, be good base fertilizer as fertilizer, but in combustion because of these alkali metal salt fusing points
It is low, it is easy slagging, dust stratification on water-cooling wall and back-end surfaces.When using circulating fluidized bed combustion mode, these sylvite meetings
The soil carried secretly with casting bed material or stalk（Containing sand）Reaction generates potassium silicate class glass, be easy to cause bed material coking or particle long
Greatly, therefore in operational process the large particle formed in combustion process should be excluded in time, supplements suitable bed material, maintain object in furnace
Material granularity it is relatively uniform.In the case that pure burning or large scale mix burning, the corrosion of the dust stratification and superheater of back-end surfaces can be non-
Chang Yanchong.In Retrofitting Heat Recovery Surface or the replacement in later period, high temperature superheater is arranged in furnace（Cross heat shielding form）, overheat
Device high temperature section uses TP347H material.It is remaining go out trailing space, low temperature superheater and economizer transverse pitch are increased, reduce by
The chance that heat area ash is put up a bridge.
Embodiment 2
The present embodiment the difference from embodiment 1 is that, further include biomass fuel co-combustion system, the biomass fuel mixes burning system
System includes the biomass fuel transportation system and coal powder conveying system of boiler two sides setting, and the biomass fuel is waste cotton slag,
The mixed-fuel burning proportion of the waste cotton slag is 10%-15%.
The exit of the high temperature cyclone separator is provided with the central tube being inserted into the high temperature cyclone separator, connection
The exhaust pass of central tube and back-end ductwork, the central tube eccentric setting.
SNCR denitrification spray gun insertion position is as shown in figure 3, be provided with two SNCR denitrification spray guns, high temperature on the reversal chamber
4 SNCR denitrification spray guns are set on Cyclone outlet flue, two SNCR denitrification spray guns, returning charges are arranged in boiler setting middle part
Two SNCR denitrification spray guns are set on pipe.Separator inlet flue cross section is smaller, and the atomized ammonia air-flow that spray gun sprays is easy to
Most of flue gas is covered, is uniformly mixed；Separator is entered after ammonium hydroxide and flue gas mixing, further in the case where flue gas stays turning effort
Mixing, and enough residence times are able to maintain so that reaction is completed；Temperature window is suitable, equipment under normal circumstances, separation
Device inlet flue gas temperature is about 920 DEG C, is suitable temperature window, and after entrance separator, which keeps very well, being conducive to ammonium hydroxide
With reacting for NOx.
Circulated air flow is provided on pipeline between the circulating fan and primary air fan entrance and secondary air fan entrance
Be provided on the pipeline in meter and circulated air regulating valve, primary air fan outlet and secondary air fan exit total airflow meter and
Total wind regulating valve.Air preheater is provided in the back-end ductwork, the primary air fan, secondary air fan pass through air preheater
It is connect respectively with First air entrance and Secondary Air entrance.It is provided with shock wave soot blower in the back-end ductwork, is set in the boiler
It is equipped with two panels water-cooling screen.
Analysis is optimized to high-speed rotational separator by numerical simulation, show that optimal case is：Central tube insertion
Depth deviates Membrane Separator Cylinder for CFB Boiler center 50- in fourth quadrant in 1700m-1800mm, entrance opening dimension 820mm*2400mm, central tube
When 100mm, central tube diameter in 1100mm-1300mm, the efficiency of the separator not only efficient pressure loss but also smaller.Do not changing
Under the premise of air compartment boiler circuit, the efficient of burning is realized.The cross-sectional structure schematic diagram of high temperature cyclone separator and boiler is such as
Shown in Fig. 4.
Influence high temperature cyclone separator separative efficiency factor include：
（1）Central tube diameter
Under identical entrance gas velocity, central tube diameter becomes smaller, and separator endoparticle tangential velocity can subtracting with central tube diameter
Small and increase, central tube entrance short circuit flow rate reduces, and is conducive to separate, and reduce the nonaxisymmetry in flow field, eddy flow is not
Stability reduces, but the overall presure drop of separator will increase.
（2）Separator inlet speed
When separator inlet speed is too low, the particle in dust does not have enough momentum, and can not collide with separator reduces momentum
It falls into separator, most of little particle can not separate, and cause under separative efficiency.When entrance velocity is excessively high, gas adds
The diffusion of play, particle increases, and causes the spring, collision, dispersion of particle, and the aggravation of solid back-mixing phenomenon is counter to decline separative efficiency,
It is unfavorable for particle separation, separative efficiency is not the raising with entrance velocity and monotone increasing；Abrasion loss and the entrance speed of separator
The direct ratio upright three times of degree, the more high then separator abrasion of inlet air flow speed is bigger, and there are optimal designs for separator inlet flow velocity
Value.
（3）Central tube insertion depth
Since eddy flow moves between central tube and wall surface, central tube length and insertion depth have larger shadow to cyclone performance
It rings.Central tube insertion is too deep, can shorten central tube at a distance from cone base, increases reentrainment chance；When central tube is inserted into
It crosses shallowly, will cause normal eddy flow core bending, be at unstable state, also easily cause gas short circuit and reduce separation and imitate
Rate.
After low nitrogen burning transformation, the combustion share of upper furnace can be improved, and flue gas temperature of hearth outlet differs very with bed temperature
Small, this is more conducive to the after-flame of temperature window and flying dust required by realizing later period SNCR.
Embodiment 3
A kind of circulating fluidized bed boiler flue gas desulfuration and denitrification remodeling method, including：
（1）Desulphurization system transformation：It transform the chimney for being used to discharge fume after original air-introduced machine as desulfurizing tower, the exit of desulfurizing tower is set
Demister is set, the inlet of desulfurization spray equipment is connect by solution feed pump with absorbent hold-up tank in desulfurizing tower, and absorbent is ammonia
Water；
（2）SNCR denitration system transformation：In desulfurizing tower be arranged SCR denitration spray equipment, the SCR denitration spray equipment into
Liquid mouth passes sequentially through ammonia air mixer, liquid ammonia vaporization device, heat exchanger, solution feed pump and reducing agent hold-up tank and connects；
（3）Feed system transformation：Waste cotton slag co-combustion system is set in boiler two sides, waste cotton slag co-combustion system includes feed bin and spiral
Batcher, the waste cotton slag in feed bin enter boiler by screw(-type) feeder, and waste cotton slag mixed-fuel burning proportion is 10%-15%；
（4）Increase flue gas recirculation system：Circulating fan is connected by pipeline at the air outlet of air-introduced machine, circulating fan passes through
Pipeline is connect with primary air fan entrance and secondary air fan entrance respectively, is followed according to the exhaust gas volumn of load control system flue gas recycled and again
The proportion of ring flue gas and First air, Secondary Air；
（5）Separation system transformation：Replace the central tube of the high temperature cyclone separator, the central tube insertion high-temp. vortex separation
Depth in device is 1700m-1800mm, the entrance opening dimension of the high temperature cyclone separator is 820mm*2400mm, central tube exists
Fourth quadrant deviates Membrane Separator Cylinder for CFB Boiler center 50-100mm, central tube diameter is 1100mm-1300mm；
（6）The SNCR system reform：Connection boiler and high temperature cyclone separator reversal chamber on be arranged two SNCR denitrification spray guns,
Be arranged on high temperature cyclone separator exhaust pass 4 SNCR denitrification spray guns, two SNCR denitrification spray guns of setting in the middle part of boiler setting,
Two SNCR denitrification spray guns are set on refeed line；
（7）Shock wave soot blower is set in back-end ductwork, increases the water-cooling screen of two panels Natural Circulation in boiler.
Claims (9)
1. a kind of circulating fluidized bed boiler flue gas desulfuration and denitrification system, including boiler, high temperature cyclone separator, back-end ductwork, institute
Boiler is stated to connect by the gas approach of reversal chamber and high temperature cyclone separator, the exhaust pass of the high temperature cyclone separator with
Back-end ductwork connection, the exhaust pass of the back-end ductwork are successively connect with deduster, air-introduced machine, the high temperature cyclone separator
Bottom connect with the return port on boiler by refeed line, which is characterized in that further include desulphurization system and denitrating system, it is described
Desulphurization system includes the desulfurizing tower with the outlet connection of air-introduced machine, and the exit of the desulfurizing tower is provided with demister, described de-
The inlet of desulfurization spray equipment is connect by solution feed pump with absorbent hold-up tank in sulphur tower, and the absorbent is ammonium hydroxide；It is described
Denitrating system includes flue gas recirculation system, SNCR denitration system and SCR denitration system, the flue gas recirculation system include with
Air-introduced machine air outlet connection circulating fan, the circulating fan by pipeline respectively with primary air fan entrance and secondary air fan
Entrance connection；The SNCR denitration system includes：The SNCR denitrification spray gun that is arranged on reversal chamber, high temperature cyclone separator outlet cigarette
The SNCR denitration being arranged in the SNCR denitrification spray gun that is arranged in the middle part of the SNCR denitrification spray gun that is arranged on road, boiler setting, refeed line
Spray gun；The SCR denitration system liquid includes the SCR denitration spray equipment in desulfurizing tower, the feed liquor of the SCR denitration spray equipment
Mouth passes sequentially through ammonia air mixer, liquid ammonia vaporization device, heat exchanger, solution feed pump and reducing agent hold-up tank and connects.
2. the circulating fluidized bed boiler flue gas desulfuration and denitrification system according to claim 1, which is characterized in that further include life
Biomass fuel co-combustion system, the biomass fuel co-combustion system include boiler two sides setting biomass fuel transportation system with
Coal powder conveying system, the biomass fuel are waste cotton slag, and the mixed-fuel burning proportion of the waste cotton slag is 10%-15%.
3. the circulating fluidized bed boiler flue gas desulfuration and denitrification system according to claim 1, which is characterized in that the high temperature
The exit of cyclone separator is provided with the central tube being inserted into the high temperature cyclone separator, connection central tube and back-end ductwork
Exhaust pass, the central tube eccentric setting.
4. the circulating fluidized bed boiler flue gas desulfuration and denitrification system according to claim 3, which is characterized in that the center
Depth in cylinder insertion high temperature cyclone separator is 1700m-1800mm, the entrance opening dimension of the high temperature cyclone separator is
820mm*2400mm, central tube deviate Membrane Separator Cylinder for CFB Boiler center 50-100mm, central tube diameter in fourth quadrant for 1100mm-
1300mm。
5. circulating fluidized bed boiler flue gas desulfuration and denitrification system according to claim 1, which is characterized in that the reversal chamber
On be provided with two SNCR denitrification spray guns, 4 SNCR denitrification spray guns, boiler settings be set on high temperature cyclone separator exhaust pass
Two SNCR denitrification spray guns are set in two SNCR denitrification spray guns of middle part setting, refeed line.
6. the circulating fluidized bed boiler flue gas desulfuration and denitrification system according to claim 1, which is characterized in that the circulation
Recirculating air flow meter and circulated air regulating valve are provided on pipeline between blower and primary air fan entrance and secondary air fan entrance,
Total airflow meter and total wind regulating valve are provided on the pipeline in the primary air fan outlet and secondary air fan exit.
7. the circulating fluidized bed boiler flue gas desulfuration and denitrification system according to claim 1, which is characterized in that the tail portion
Be provided with air preheater in flue, the primary air fan, secondary air fan by air preheater respectively with First air entrance and
The connection of Secondary Air entrance.
8. the circulating fluidized bed boiler flue gas desulfuration and denitrification system according to claim 1, which is characterized in that the tail portion
It is provided with shock wave soot blower in flue, two panels water-cooling screen is provided in the boiler.
9. a kind of circulating fluidized bed boiler flue gas desulfuration and denitrification remodeling method, which is characterized in that including：
（1）Desulphurization system transformation：It transform the chimney for being used to discharge fume after original air-introduced machine as desulfurizing tower, the exit of desulfurizing tower is set
Demister is set, the inlet of desulfurization spray equipment is connect by solution feed pump with absorbent hold-up tank in desulfurizing tower, and absorbent is ammonia
Water；
（2）SNCR denitration system transformation：SCR denitration spray equipment is set in desulfurizing tower, the SCR denitration spray equipment
Inlet passes sequentially through ammonia air mixer, liquid ammonia vaporization device, heat exchanger, solution feed pump and reducing agent hold-up tank and connects；
（3）Feed system transformation：Waste cotton slag co-combustion system is set in boiler two sides, waste cotton slag co-combustion system includes feed bin and spiral
Batcher, the waste cotton slag in feed bin enter boiler by screw(-type) feeder, and waste cotton slag mixed-fuel burning proportion is 10%-15%；
（4）Increase flue gas recirculation system：Circulating fan is connected by pipeline at the air outlet of air-introduced machine, circulating fan passes through
Pipeline is connect with primary air fan entrance and secondary air fan entrance respectively, is followed according to the exhaust gas volumn of load control system flue gas recycled and again
The proportion of ring flue gas and First air, Secondary Air；
（5）Separation system transformation：Replace the central tube of the high temperature cyclone separator, the central tube insertion high-temp. vortex separation
Depth in device is 1700m-1800mm, the entrance opening dimension of the high temperature cyclone separator is 820mm*2400mm, central tube exists
Fourth quadrant deviates Membrane Separator Cylinder for CFB Boiler center 50-100mm, central tube diameter is 1100mm-1300mm；
（6）The SNCR system reform：Connection boiler and high temperature cyclone separator reversal chamber on be arranged two SNCR denitrification spray guns,
Be arranged on high temperature cyclone separator exhaust pass 4 SNCR denitrification spray guns, two SNCR denitrification spray guns of setting in the middle part of boiler setting,
Two SNCR denitrification spray guns are set on refeed line；
（7）Shock wave soot blower is set in back-end ductwork, increases the water-cooling screen of two panels Natural Circulation in boiler.
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| CN114877318A (en) * | 2022-05-31 | 2022-08-09 | 西安华电清洁能源技术有限公司 | Circulating fluidized bed boiler nitrogen oxide removal process system suitable for deep peak regulation |
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