CN110354677A - It is a kind of sintering, pelletizing head flue gas emission purification system - Google Patents
It is a kind of sintering, pelletizing head flue gas emission purification system Download PDFInfo
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- CN110354677A CN110354677A CN201910600271.3A CN201910600271A CN110354677A CN 110354677 A CN110354677 A CN 110354677A CN 201910600271 A CN201910600271 A CN 201910600271A CN 110354677 A CN110354677 A CN 110354677A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 164
- 239000003546 flue gas Substances 0.000 title claims abstract description 162
- 238000005453 pelletization Methods 0.000 title claims abstract description 35
- 238000005245 sintering Methods 0.000 title claims abstract description 30
- 238000000746 purification Methods 0.000 title claims abstract description 21
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 60
- 230000023556 desulfurization Effects 0.000 claims abstract description 55
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 18
- 238000005406 washing Methods 0.000 claims abstract description 10
- 238000004140 cleaning Methods 0.000 claims abstract description 9
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000000908 ammonium hydroxide Substances 0.000 claims abstract description 5
- 239000006200 vaporizer Substances 0.000 claims abstract description 3
- 238000001816 cooling Methods 0.000 claims description 31
- 239000003517 fume Substances 0.000 claims description 28
- 239000002002 slurry Substances 0.000 claims description 22
- 229910000831 Steel Inorganic materials 0.000 claims description 15
- 239000010959 steel Substances 0.000 claims description 15
- 239000007921 spray Substances 0.000 claims description 12
- 239000006096 absorbing agent Substances 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 10
- 230000005494 condensation Effects 0.000 claims description 10
- 235000019504 cigarettes Nutrition 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000005260 corrosion Methods 0.000 claims description 6
- 230000007797 corrosion Effects 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 6
- 229920002313 fluoropolymer Polymers 0.000 claims description 5
- 230000001413 cellular effect Effects 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 43
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 37
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 26
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 25
- 229910021529 ammonia Inorganic materials 0.000 abstract description 16
- 238000005516 engineering process Methods 0.000 abstract description 13
- 238000010531 catalytic reduction reaction Methods 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 8
- 239000013618 particulate matter Substances 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 6
- MXWHMTNPTTVWDM-NXOFHUPFSA-N mitoguazone Chemical compound NC(N)=N\N=C(/C)\C=N\N=C(N)N MXWHMTNPTTVWDM-NXOFHUPFSA-N 0.000 abstract description 6
- 239000002245 particle Substances 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 description 7
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 5
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 5
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 5
- 239000000779 smoke Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 235000011130 ammonium sulphate Nutrition 0.000 description 4
- 239000003337 fertilizer Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- 206010013786 Dry skin Diseases 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 235000013399 edible fruits Nutrition 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
-
- 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
-
- 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
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention provides a kind of sintering, pelletizing head flue gas emission purification system, specifically include that water-borne formula flue gas heat-exchange unit (MGGH), desulfurizing tower, flue gas condenser, rotary flue gas heat-exchange unit (GGH), flue combustor/hot-blast stove, ammonium hydroxide vaporizer, denitrification apparatus, booster fan, chimney.The present invention uses the ammonia process of desulfurization and selective-catalytic-reduction denitrified (SCR) technology, realizes sulfur dioxide, nitrogen oxides and particulate matter minimum discharge and flue gas disappears white purpose.Ammonia process of desulfurization effect is improved by ultrasonic wave swirling flow atomizing technology；By water washing cleaning section and flue gas condensing technology, exit gas temperature and particle content after desulfurization are reduced, flue gas water content is reduced, reduces system water consumption；Reduce energy consumption needed for denitration by rotary flue gas heat-exchange unit, and improve flue gas emission final temperature, it is white to realize that flue gas disappears；Process route is simple, easy to operate.
Description
Technical field
The present invention relates to environment protection fields, and in particular to flue gases purification, especially a kind of sintering, pelletizing head flue gas row
Purification system is put, environmentally friendly (gas cleaning) technical field is belonged to.
Background technique
In steel industry or other industrial productions, the flue gas that the burning between raw material and fuel generates contains a large amount of nitrogen
Oxide, sulfur dioxide and particulate matter cause certain pollution to atmosphere.Five ministries and commissions such as ecological environment in April, 2019 portion connection
Conjunction is printed and distributed " about the opinion for implementing steel industry minimum discharge is promoted ", the target and index being clearly transformed.Wherein index is as follows:
Pelletizer head, pellet roasting flue gas particles, sulfur dioxide, the small hourly value of discharged nitrous oxides concentration be respectively no higher than 10,
35, (sintering machine head end, palletizing shaft furnace benchmark oxygen content are 16% to 50 milligrams/cubic metre, grate kiln, belt pellet roasting
18%) machine benchmark oxygen content is；The small hourly value of other primary pollution source particulate matters, sulfur dioxide, discharged nitrous oxides concentration is former
Then upper respectively no higher than 10,50,200 milligrams/cubic metre.
Steel industry is sintered, the removal methods of pelletizing SO 2 from fume mainly have wet process, dry method and semidry method, wherein wet
Law technology is mainly limestone-gypsum method, ammonia process, magnesium oxide method, double neutralizing treatment methods etc..Sintering, pelletizing head flue gas wet process are de-
Sulphur Technical comparing is mature, is calcium method and ammonia process using more technique, and wherein ammonia process of desulfurization efficiency can achieve 98% or more,
Using ammonium hydroxide as desulfurizing agent, (NH is used4)2SO3、(NH4)2SO4、NH3HSO3Mixed solution carry out cyclic absorption SO2, to reach
To removal SO2Purpose.Flue gas after desulfurization is washed by water washing cleaning, and the means such as dedusting demisting and flue gas condensing will wherein
Contained drop and particulate matter captures, and reduces moisture content, realizes the minimum discharge of sulfur dioxide and particulate matter.Desulfurization
Certain density ammonium sulfate obtained by journey enters sulphur ammonium preparation system, obtains finished product sulphur by techniques such as evaporation, crystallization, dryings
Sour ammonium fertilizer.
The removal methods of nitrogen oxides mainly have reduction method, oxidizing process and decomposition method.Selective non-catalytic in reduction method
It restores (SNCR) and selective catalytic reduction (SCR) is considered as most effective denitration technology, can satisfy stringent flue gas row
Put standard.Steel enterprise sintering, pelletizing head flue-gas temperature be generally at 120-160 DEG C at present, not selective non-catalytic also
Former (SNCR) and selective catalytic reduction (SCR) Process window temperature range, but by combustion-compensating device/hot-blast stove, and utilize
Rotary flue gas heat-exchange unit may be implemented less energy consumption and promote pelletizing flue-gas temperature to 200-320 DEG C, to reach low, medium temperature
SCR Process window temperature.Under the conditions of this temperature, reducing agent ammonia is sprayed into flue gas, under the effect of the catalyst ammonia and flue gas
In reaction of nitrogen oxides and generate nontoxic, free of contamination nitrogen and water, to realize the minimum discharge of nitrogen oxides, meanwhile,
Discharged gas fume temperature can be improved to 95-130 DEG C in rotary flue gas heat-exchange unit, realizes that discharged gas fume disappears white effect.Sintering, pelletizing
Head flue gas emission purification system disappears white in the minimum discharge and flue gas for realizing sulfur dioxide, nitrogen oxides and particulate matter
In whole process, by-product is ammonium sulfate fertilizer, is generated without waste water, waste residue and exhaust gas, and the environmental protection of green, circular economy is belonged to
Means.
Summary of the invention
The present invention provides a kind of flue gas emission purification system, main using the ammonia process of desulfurization and selective-catalytic-reduction denitrified
(SCR) technology, with realize SO 2 from fume, nitrogen oxides and particulate matter minimum discharge and flue gas disappear it is white for the purpose of.
For this purpose, the present invention proposes a kind of (sintering, pelletizing head) flue gas emission purification system, flue gas emission purification system
System includes:
Water-borne formula flue gas heat-exchange unit (MGGH), has warming-up section and temperature descending section, and temperature descending section is arranged in main exhauster to desulfurization
On the flue of tower entrance, temperature descending section connects the flue after the pelletizing main exhauster；Warming-up section setting is exported to back in desulfurizing tower
On the flue of rotatable flue gas heat-exchange unit former fume side import (first entrance), warming-up section connects the rotary flue gas heat-exchange unit.
Desulfurizing tower connects the water-borne formula flue gas heat-exchange unit temperature descending section；
Flue gas condenser connects the desulfurizing tower；
Water-borne formula flue gas heat-exchange unit warming-up section, connects the flue gas condenser；
Rotary flue gas heat-exchange unit has former fume side import (first entrance), former fume side outlet (first outlet), net
Smoke inlet (second entrance) and neat stress side outlet (second outlet), rotary flue gas heat-exchange unit former fume side import connect institute
State water-borne formula flue gas heat-exchange unit warming-up section；
Flue combustor/hot-blast stove is arranged in the flue of the rotary flue gas heat-exchange unit former fume side outlet；Or it adopts
With hot-blast stove, it is connected on the flue of the rotary flue gas heat-exchange unit former fume side outlet；
Ammonium hydroxide vaporizer connects on the rotary flue gas heat-exchange unit former fume side exhaust pass；
Benitration reactor connects the former fume side exhaust pass；
The second entrance of rotary flue gas heat-exchange unit connects the Benitration reactor；
Booster fan connects the second outlet of rotary flue gas heat-exchange unit；
Rotary flue gas heat-exchange unit neat stress entrance, connects the Benitration reactor；
Rotary flue gas heat-exchange unit neat stress outlet, connects the rotary flue gas heat-exchange unit neat stress entrance；
Booster fan connects rotary flue gas heat-exchange unit neat stress side outlet；
Chimney connects the booster fan outlet.
Further, the desulfurizing tower includes: the cooling enriching section of 1 section of independent loops, and train operation density index is in 1.15-
1.18g/cm3, the density index that discharges is in 1.20-1.30g/cm3；The absorber portion of 1-2 sections of independent loops, train operation density index exist
1.05-1.11g/cm3；The water washing cleaning section of 1-3 sections of independent loops, train operation density index is in 1.01-1.03g/cm3；System uses
Ammonium hydroxide is arranged high efficiency demister between each independent loops section, slurries is avoided to carry secretly as total liquid-gas ratio >=9.
Further, the desulphurization system include: be arranged in desulfurizing tower cooling enriching section or absorber portion side wall on it is multiple
Rotational flow atomizer.
Further, the multiple rotational flow atomizer is arranged in tangential in same level on desulfurization tower side wall.
Further, it by being arranged on desulfurization tower side wall in multiple rotational flow atomizers that same level is tangential, is formed
Swirl-spray layer.When rotational flow atomizer is arranged in cooling enriching section, on the one hand by desulfurizing agent partial size by traditional spraying layer
1500-3000 μm drops to 50-150 μm, and same desulfurization slurry specific grain surface product improves more than 400 to 900 times, makes desulfurization absorptance
Surface area increases, and reaction speed is accelerated, and realizes the high-efficiency desulfurization in the case where small liquid-gas ratio, reduces desulfurization energy consumption；It is another
Aspect constructs desulfurizing tower internal spraying eddy flow field, forms high-speed rotating cloud and mist due to using atomizing eddy flow circle of contact placement technique
Shape, flue gas is full and uniform with desulphurizer mixing, increases SO in flue gas2With reactive desulfurizing agent probability, desulfuration efficiency is improved.Eddy flow
Spraying layer not only has the function of countercurrent spray layer, the function of more standby efficiently turbulent flow reaction.The reconstruction of cloud flow field is realized, is formed
Stablize rotation air film stabilized zone in desulfurizing tower, eliminates the smoke corridor problem in conventional spray column, further increase cooling, remove
Dirt and desulfuration efficiency reduce aerosol and generate.
Further, the water-borne formula flue gas heat-exchange unit further include: temperature descending section and warming-up section are all made of corrosion resisting steel H wing
Leaf form；Temperature descending section is arranged in front of desulfurizing tower on flue, and desulfurizing tower entrance flue gas temperature is reduced 30-40 DEG C；Warming-up section arrangement
After flue gas condenser, desulfurizing tower exit gas temperature is increased 30-40 DEG C.
Further, the flue gas condenser includes 2 kinds of schemes: 1. by setting in cooling enriching section/absorber portion/water
Slurry temperature is reduced 5-10 DEG C, after cooling by the slurry heat exchanger (using board-like or corrosion-resisting tubular steel heat exchanger) for washing clean-up stage
Slurries acted on by spray, desulfurization fume is condensed from 53-55 DEG C of cooling to 45-48 DEG C.2. being gone out by being arranged in desulfurizing tower
Independent condenser (using fluoroplastics or corrosion resisting steel) on mouthful flue carries out condensation cooling to flue gas, directly by desulfurization fume from
53-55 DEG C of cooling condensation is to 45-48 DEG C.Flue gas condenser is using the one of which in 2 kinds of schemes.
Further, when flue gas is by condensation dedusting demister, temperature is lowered 5-10 DEG C, reduces saturated flue gas band water
Rate reduces system water consume, disappears conducive to protection rear end denitration GGH and flue gas white.
Further, the denitrification apparatus is arranged in after desulfurizing tower.
Further, the denitrification apparatus further include: catalyst is using board-like or cellular, the bed designs 2+1 of wide temperature
Or 3+1 mode.
Further, the denitrification apparatus further include: 200-320 DEG C of adjustable range of denitration reaction temperature design, have good
Good adaptability.
Further, the rotary flue gas heat-exchange unit further include: rotary flue gas heat-exchange unit neat stress exiting flue gas temperature
Degree reaches 95-130 DEG C, and it is white to realize that flue gas disappears.
Ammonia desulfurizing process is preferably combined selective catalytic reduction (SCR) denitration technology by the present invention, using first desulfurization
The process route of denitration afterwards.Flue-gas temperature in tower is reduced using MGGH cooperation rotational flow atomizer, is conducive to the ammonia process of desulfurization and controls, improve
Desulfuration efficiency reduces the escaping of ammonia, and improves flue-gas temperature after flue gas condenser, and denitration GGH is protected not corroded；It is cold using flue gas
Condenser further decreases saturated flue gas temperature and water content after desulfurization, reduces system water consumption；Using denitration GGH, realize compared with
Sintering after desulfurization, pelletizing flue gas are promoted to selective-catalytic-reduction denitrified Process window temperature by low energy expenditure, and are improved
It is white to realize that flue gas disappears for the final exhaust temperature of flue gas after denitration.Whole device process route is simple, easy to operate, to energy-saving and emission-reduction, ring
Border protection, the technologies such as by-product resource are all the important breakthroughs in sintering, pelletizing filed of flue gas purification.
Detailed description of the invention
Fig. 1 is the working principle of the invention schematic diagram.
1, sintering, pelletizing main exhauster；2, water-borne formula flue gas heat-exchange unit (temperature descending section)；3, water-borne formula flue gas heat-exchange unit (rises
Temperature section)；4, desulfurizing tower (containing rotational flow atomized spray injector, multi-section circulation)；5, flue gas condenser；6,GGH；7, hot-blast stove/flue burning
Device；8, denitrification apparatus (containing catalyst)；9, booster fan；10, chimney.
Specific embodiment
For a clearer understanding of the technical characteristics, objects and effects of the present invention, this hair of Detailed description of the invention is now compareed
It is bright.Technical principle of the invention
Desulfurization principle:
NH3+SO2+H2O=NH4HSO3
2NH3+SO2+H2O=(NH4)2SO3
(NH4)2SO3+SO2+H2O=2NH4HSO3(desulfurization key reaction)
NH4HSO3+NH3=(NH4)2SO3
Denitration principle:
4NO+4NH3+O2→4N2+6H2O
2NO2+4NH3+O2→3N2+6H2O
Flue gas heating, cooling principle: 1. by water-borne formula flue gas heat-exchange unit (MGGH) by the sintering of desulfurization entrance, pelletizer
Head flue gas heat passes to neat stress after desulfurization, so that reaching reduces desulfurization inlet flue gas temperature, and improves the effect of desulfurization outlet smoke temperature
Fruit；2. high temperature sintering, pelletizing head flue gas heat after denitration are passed to denitration entrance by rotary flue gas heat-exchange unit (GGH)
Pelletizing original flue gas, thus reach improve denitration inlet flue gas temperature, reduce afterburner energy consumption effect；
Desulfurization fume condensation principle: 1. will cooling by slurry heat exchanger (using board-like or corrosion-resisting tubular steel heat exchanger)
Enriching section/absorber portion/water washing cleaning section loop slurry cools down, and the loop slurry after cooling again sprays desulfurization fume
Leaching cooling.2. desulfurizing tower is exported cigarette by independent condenser (using fluoroplastics or the tube heat exchanging component of corrosion resisting steel material)
Gas directly carries out condensation cooling.
Further, when flue gas is by condensation dedusting demister, temperature is lowered 5-10 DEG C, reduces saturated flue gas band water
Rate reduces system water consume, disappears conducive to protection rear end denitration GGH and flue gas white.
The present invention utilizes the ammonia process of desulfurization, selective catalytic reduction, and by water-borne formula flue gas heat-exchange unit and returns
Rotatable flue gas heat-exchange unit reduces and increases the flue-gas temperature of each functional area, and sintering, pelletizer are realized under lower energy consumption condition
Head SO 2 from fume, nitrogen oxides and remove the ultra-clean discharge of particulate matter.
The detailed process that the present invention realizes: as shown in Figure 1,
(1) rotary flue gas heat-exchange unit (GGH) (rotary flue gas is configured in denitrification apparatus (containing catalyst) 7 downstreams
Heat exchanger 5)；
(2) sintering, (120-160 DEG C) of the pelletizing original flue gas water-borne formula flue gas heat-exchange unit of entrance is made to cool down by booster fan 8
Section 2 enters desulfurizing tower 3 after pelletizing original flue-gas temperature is reduced 30-40 DEG C；
(3) flue gas in desulfurizing tower with common desulphurization slurries (1500-3000 μm of partial size) and swirling flow atomizing desulfurization slurry (grain
50-150 μm of diameter) cooling dedusting and desulfurization absorption are carried out, then after 1-3 grades of washings, then it is further by flue gas condenser
Flue gas after desulfurization temperature is reduced to 45-48 DEG C, not only reduces saturated flue gas water amount, also subsidiary secondary deep dedusting function.
Slurries obtained by desulfurization are sent after peroxidating, concentration to sulphur ammonium preparation system, and sulfuric acid is made using techniques such as evaporation, crystallization and dryings
Ammonium product.
(4) enter water-borne formula flue gas heat-exchange unit warming-up section 4 by desulfurizing tower treated desulfurization neat stress, by the net cigarette of desulfurization
Temperature degree improves 30-40 DEG C, and desulfurization neat stress becomes undersaturated condition by saturation.
(5) the desulfurization neat stress after the heating of water-borne formula flue gas heat-exchange unit enters rotary flue gas heat-exchange unit (denitration original cigarette
Gas side) flue gas (200-320 DEG C) that enters rotary flue gas heat-exchange unit (denitration neat stress side) behind 5, with denitration exchanges heat, temperature
Degree rises to 170-295 DEG C；
(3) the denitration original flue gas after the heat exchange heating of rotary flue gas heat-exchange unit is heated up by hot-blast stove or combustion-compensating device 6
To 200-320 DEG C, the flue gas containing ammonia then come with dilution air is uniformly mixed；
(4) enter denitrification apparatus 7 with the mixed uniformly denitration original flue gas of ammonia, the wide temperature catalyst inside denitrification apparatus
Under active catalytic effect, ammonia is by NOXIt is reduced into N2And H2O realizes the remove of nitrogen oxides；
(5) the high temperature denitration neat stress (200-320 DEG C) after denitration changes heat by rotary flue gas heat-exchange unit (GGH)
Pelletizing original flue gas is given, temperature is down to 95-130 DEG C；
(6) the denitration neat stress after cooling down enters booster fan 8, and booster fan 8 can overcome the resistance of whole system to make
With.
(7) the denitration neat stress after booster fan 8 is discharged into atmosphere through chimney 9, and without obvious white cigarette phenomenon.
In the present invention, each stage technique main points:
(1) combined with selective catalytic reduction (SCR) using the ammonia process of desulfurization, after elder generation's desulfurization denitration technique
Route.
(2) desulfurization technology: efficient ammonia-process desulfurization technique is 1. used, by-product is ammonium sulfate fertilizer, entire production process
No waste water, waste generate, and realize the resource utilization of byproduct.2. selection high-efficiency cyclone atomizer tower inscribed circle arrange into
Row cooling dedusting or desulfurization, form swirl-spray layer, desulfurization slurry partial size is by common 1500-3000 μm in desulfurizing tower plane
50-150 μm is dropped to, same desulfurization slurry specific surface area improves more than 400 to 900 times, and so that desulfurization is absorbed specific surface area and increases, reaction
Speed is accelerated.Swirl-spray layer has the function of efficiently turbulent flow reaction, realizes the reconstruction of cloud flow field, is formed and stablize rotation in desulfurizing tower
Turn air film stabilized zone, eliminates the smoke corridor problem in conventional spray column, further increase cooling, dedusting and desulfuration efficiency.
3. the cooling enriching section of 1 section of independent loops is arranged in desulfurizing tower, train operation density index is in 1.15-1.18g/cm3, discharge density index
In 1.20-1.30g/cm3；The absorber portion of 1-2 sections of independent loops, train operation density index is in 1.05-1.11g/cm3；1-3 sections independent
The water washing cleaning section of circulation, train operation density index is in 1.01-1.03g/cm3；Total liquid-gas ratio >=9 of system, in each independent loops section
Between high efficiency demister is set, avoid slurries from carrying secretly.
(3) denitration technology: 1. use efficient selective catalytic reduction (SCR), by-product be nitrogen and water,
No other waste water, waste generate.2. selection has the warm catalyst of the width of preferable adaptability, well-defined reaction temp section is 200-320
DEG C, it can be used board-like or cellular, bed designs are 2+1 or 3+1 mode, avoid catalyst from blocking, poisoning and inactivation occur existing
As.
(4) flue gas heating, cooling heat utilization technology: by water-borne formula flue gas heat-exchange unit (MGGH) by the burning of desulfurization entrance
Knot, pelletizing head original flue gas heat pass to neat stress after desulfurization, so that reaching reduces desulfurization inlet flue gas temperature, and improve desulfurization and go out
The effect of mouth smoke temperature；2. the net head flue gas heat of high temperature sintering, pelletizing after denitration is passed by rotary flue gas heat-exchange unit (GGH)
Sintering, the pelletizing head original flue gas of denitration entrance are passed, denitration inlet flue gas temperature is improved to reach, reduces the effect of afterburner energy consumption
Fruit；
(5) flue gas condensing technology: 1. will cooling by slurry heat exchanger (using board-like or corrosion-resisting tubular steel heat exchanger)
Enriching section/absorber portion/water washing cleaning section loop slurry cools down, and the loop slurry after cooling again sprays desulfurization fume
Leaching cooling.2. desulfurizing tower is exported cigarette by independent condenser (using fluoroplastics or the tube heat exchanging component of corrosion resisting steel material)
Gas carries out condensation cooling.
Specific embodiment:
2 × 500m of Guangxi steel enterprise Co., Ltd2Sintering and 4,000,000 tons/year of flue gas desulfurizations of pelletizing head, denitration items
Mesh, design exhaust gas volumn are divided into 180 × 104Nm3/ h (separate unit 500m2Sintering) and 125 × 104Nm3/ h, particle concentration are 50
㎎/Nm3, sulfur dioxide concentration is 2000 ㎎/Nm3, nitrous oxides concentration is 400 ㎎/Nm3, using process flow are as follows: burn
Knot, pelletizing head flue gas → head electric precipitator → main exhauster 1 → 2 → desulfurizing tower of water-borne formula flue gas heat-exchange unit temperature descending section 4 (packet
Cooling dedusting, absorption and water washing cleaning are included, and using rotational flow atomizer technology etc.) → flue gas condenser 5 → water-borne formula flue gas
Heat exchanger (MGGH) warming-up section 3 → 6 (denitration former fume side) → hot-blast stove/flue combustor 7 of rotary flue gas heat-exchange unit → de-
Nitre device 8 → rotary flue gas heat-exchange unit 6 (denitration neat stress side) → 9 → chimney of booster fan 10, whole process passes through to cigarette
Gas cools down and heats up twice, realizes to the high-efficiency desulfurization of flue gas, denitration, dedusting, demisting and disappears white.Preferably by chimney outlet
Particle concentration is less than 10 ㎎/Nm3, sulfur dioxide concentration is less than 35 ㎎/Nm3, nitrous oxides concentration is less than 50 ㎎/Nm3, dedusting
Efficiency is greater than 80%, and desulfuration efficiency is greater than 98.5%, and denitration efficiency is greater than 87.5%, 120-125 DEG C of exhaust gas temperature, realizes flue gas
Disappear white, meet national minimum discharge standard, while obtaining ammonium sulfate fertilizer byproduct, realizes the circulation warp of by-product resource
Ji.
The foregoing is merely the schematical specific embodiment of the present invention, the range being not intended to limit the invention.For this
Each component part of invention can be combined with each other under conditions of not conflicting, any those skilled in the art, not depart from this
Made equivalent changes and modifications, should belong to the scope of protection of the invention under the premise of the conceptions and principles of invention.
Claims (10)
1. a kind of sintering, pelletizing head flue gas emission purification system, which is characterized in that the flue gas emission purification system includes:
Water-borne formula flue gas heat-exchange unit, has warming-up section and temperature descending section, and the cigarette of main exhauster to desulfurizing tower entrance is arranged in temperature descending section
On road, temperature descending section connects the flue after the pelletizing main exhauster；Warming-up section setting is exported to rotary flue gas in desulfurizing tower and changes
Hot device former fume side import, i.e., on the flue of first entrance, warming-up section connects the flue gas condenser；
Desulfurizing tower connects the water-borne formula flue gas heat-exchange unit temperature descending section；
Flue gas condenser connects the desulfurizing tower；
Water-borne formula flue gas heat-exchange unit warming-up section, connects the flue gas condenser；
Rotary flue gas heat-exchange unit has former fume side import, i.e. first entrance, former fume side outlet, i.e. first outlet, net cigarette
Gas entrance, i.e. second entrance and neat stress side outlet, i.e. second outlet, rotary flue gas heat-exchange unit former fume side import connect institute
State water-borne formula flue gas heat-exchange unit warming-up section；
Flue combustor/hot-blast stove is arranged in the flue of the rotary flue gas heat-exchange unit former fume side outlet；Or using heat
Wind furnace is connected on the flue of the rotary flue gas heat-exchange unit former fume side outlet；
Ammonium hydroxide vaporizer connects on the rotary flue gas heat-exchange unit former fume side exhaust pass；
Benitration reactor connects the former fume side exhaust pass；
The second entrance of rotary flue gas heat-exchange unit connects the Benitration reactor；
Booster fan connects the second outlet of rotary flue gas heat-exchange unit；
Rotary flue gas heat-exchange unit neat stress entrance, connects the Benitration reactor；
Rotary flue gas heat-exchange unit neat stress outlet, connects the rotary flue gas heat-exchange unit neat stress entrance；
Booster fan connects rotary flue gas heat-exchange unit neat stress side outlet；
Chimney connects the booster fan outlet.
2. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that the desulfurizing tower packet
Include: the cooling enriching section of 1 section of independent loops, train operation density index is in 1.15-1.18g/cm3, the density index that discharges is in 1.20-
1.30g/cm3；The absorber portion of 1-2 sections of independent loops, train operation density index is in 1.05-1.11g/cm3；The water of 1-3 sections of independent loops
Clean-up stage is washed, train operation density index is in 1.01-1.03g/cm3；Demister is set between each independent loops section, slurries is avoided to press from both sides
Band.
3. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that the desulphurization system
It include: the multiple rotational flow atomizers being arranged on desulfurizing tower absorber portion side wall, the desulfurization slurry partial size that atomizer sprays is 50-
150μm。
4. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that the multiple eddy flow
Atomizer is arranged in tangential in same level on desulfurizing tower absorber portion side wall.
5. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that the temperature descending section and
Warming-up section, using corrosion resisting steel band H-type wing leaf pipe or fluoroplastics tubular type；Desulfurizing tower entrance flue gas temperature is reduced 30- by temperature descending section
40 DEG C, flue gas condenser exit gas temperature is increased 30-40 DEG C by warming-up section.
6. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that the flue gas condensing
Device, for one of following 2 kinds of schemes: first is that by the way that cooling enriching section/absorber portion/water washing cleaning section slurries heat exchange is arranged in
Slurry temperature is reduced 5-10 DEG C, the slurries after cooling are made by spray using board-like or corrosion-resisting tubular steel heat exchanger by device
With by desulfurization fume from 53-55 DEG C of cooling condensation to 45-48 DEG C；Second is that passing through the independence being arranged on desulfurizing tower exhaust pass
Flue gas condenser, flue gas condenser use corrosion resisting steel or fluoroplastics material, condensation cooling are carried out to flue gas, directly by desulfurization cigarette
Gas is from 53-55 DEG C of cooling condensation to 45-48 DEG C.
7. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that denitrification apparatus arrangement
After desulfurizing tower.
8. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that the denitrification apparatus
In, catalyst is board-like or cellular using wide temperature, and bed designs are 2+1 or 3+1 mode.
9. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that the denitrification apparatus
In, 200-320 DEG C of adjustable range of denitration reaction temperature design.
10. sintering as described in claim 1, pelletizing head flue gas emission purification system, which is characterized in that the booster fan
It is arranged after denitrification apparatus, booster fan uses axial-flow type.
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