CN109331649A - Coke oven flue gas semi-dry desulphurization, dedusting and low-temperature denitration device and its process - Google Patents
Coke oven flue gas semi-dry desulphurization, dedusting and low-temperature denitration device and its process Download PDFInfo
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- CN109331649A CN109331649A CN201811401019.1A CN201811401019A CN109331649A CN 109331649 A CN109331649 A CN 109331649A CN 201811401019 A CN201811401019 A CN 201811401019A CN 109331649 A CN109331649 A CN 109331649A
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- flue gas
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- coke oven
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- 239000003546 flue gas Substances 0.000 title claims abstract description 106
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 101
- 239000000571 coke Substances 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 43
- 230000003009 desulfurizing Effects 0.000 claims abstract description 43
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 33
- 238000005516 engineering process Methods 0.000 claims abstract description 14
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 51
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 51
- 239000002250 absorbent Substances 0.000 claims description 33
- 230000002745 absorbent Effects 0.000 claims description 33
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 32
- 239000000908 ammonium hydroxide Substances 0.000 claims description 28
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 27
- 239000002002 slurry Substances 0.000 claims description 25
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 238000001704 evaporation Methods 0.000 claims description 17
- 239000000428 dust Substances 0.000 claims description 15
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 15
- 238000010521 absorption reaction Methods 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 239000001187 sodium carbonate Substances 0.000 claims description 12
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 10
- 239000000920 calcium hydroxide Substances 0.000 claims description 10
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 9
- 239000006071 cream Substances 0.000 claims description 8
- 238000004537 pulping Methods 0.000 claims description 7
- 239000003638 reducing agent Substances 0.000 claims description 7
- QAOWNCQODCNURD-UHFFFAOYSA-L sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 7
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 6
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 6
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 6
- 235000012204 lemonade/lime carbonate Nutrition 0.000 claims description 6
- 239000000843 powder Substances 0.000 claims description 6
- 235000019504 cigarettes Nutrition 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 5
- 239000011575 calcium Substances 0.000 claims description 4
- 239000007795 chemical reaction product Substances 0.000 claims description 4
- 239000003517 fume Substances 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 4
- 229910052717 sulfur Inorganic materials 0.000 claims description 4
- 239000011593 sulfur Substances 0.000 claims description 4
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 210000003850 cellular structures Anatomy 0.000 claims description 3
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 3
- 238000001694 spray drying Methods 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- 238000000746 purification Methods 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 4
- 239000002893 slag Substances 0.000 abstract description 3
- 238000005507 spraying Methods 0.000 abstract description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 239000011269 tar Substances 0.000 description 6
- 238000004939 coking Methods 0.000 description 5
- 229940095054 Ammoniac Drugs 0.000 description 4
- 229910002089 NOx Inorganic materials 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- 230000001590 oxidative Effects 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- BIGPRXCJEDHCLP-UHFFFAOYSA-N Ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 229910052813 nitrogen oxide Inorganic materials 0.000 description 3
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous Oxide Chemical class [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 230000000607 poisoning Effects 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- GBAOBIBJACZTNA-UHFFFAOYSA-L Calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 210000004080 Milk Anatomy 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N Sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- 235000015450 Tilia cordata Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking Effects 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000001413 cellular Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atoms Chemical class [H]* 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 230000002427 irreversible Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000008267 milk Substances 0.000 description 1
- 235000013336 milk Nutrition 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 230000000149 penetrating Effects 0.000 description 1
- 230000002441 reversible Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
-
- 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
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- 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
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
-
- 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 a kind of coke oven flue gas semi-dry desulphurization, dedusting and low-temperature denitration device and its processes, belong to flue gas and need purification device technical field.The present invention includes the coke oven being sequentially connected by flue, semi-dry desulphurization tower, bag filter, SCR reactor, air-introduced machine and chimney, rotary atomizer is installed on semi-dry desulphurization top of tower, tower bottom unloading valve is installed at semi-dry desulphurization tower the taper bucket, bag filter bottom is equipped with screw conveyor, it is connect by drag conveyor and bucket elevator with grey library, the lower part Hui Ku ash bucket is provided with unloading valve.The present invention uses rotating spraying semi-dry desulphurization technology, non-wastewater discharge, and desulfurization slag has stable market channel, thoroughly solves environmental issue;Discharge is without white haze trailing phenomenon;Improve the service life of low temperature catalyst.The present invention can be widely used in flue gas and need purification device occasion, be particularly suitable for the low-temperature denitrations such as coke oven, waste incinerator, Industrial Stoves, desulfurization and dedusting field.
Description
Technical field
The present invention relates to a kind of coke oven flue gas semi-dry desulphurization, dedusting and low-temperature denitration device and its processes, belong to
Flue gas needs purification device technical field.
Background technique
The coke oven flue gas in the production of country's coking industry coke oven for coke oven heating summarizes meeting by main chimney flue at present
It is discharged directly to the atmosphere by chimney.The atmosphere pollution of coke oven smoke stack emission is the exhaust gas generated after coke-stove gas burns, main
There is SO2、NOxAnd flue dust etc., pollutant are to pollute one of industry the most serious in organized overhead point source continuity discharge.
In June, 2012, Environmental Protection Department and national quality supervision and inspection Quarantine Bureau, which combine, has issued " coking chemistry industry dirt
Contaminate object discharge standard " (GB16171-2012), the clear stipulaties atmosphere pollutants emission standards of coking industry.The year two thousand twenty Shandong
It is higher to save regional Air Pollutant Emission comprehensive standard (DB37/2376-2013) the 4th period key area emission request.It wants
Seek regulation SO2Concentration of emission≤50mg/Nm3、NOxConcentration of emission≤100mg/Nm3, granular material discharged concentration≤10mg/Nm3。
Coke oven construction is more special, different from traditional coal-burning boiler, and coke oven flue gas and coal-fired electric generation furnace Gas phase Smoke ratio
Make a marked difference feature, for example coke oven flue gas sulfur dioxide concentration is relatively low, and nitrous oxides concentration is relatively high, flue gas
Middle dust content is low, but moisture content height etc..And coke oven exit gas temperature is different from coal-burning boiler, coke oven exiting flue gas temperature
Degree between 230~300 DEG C, at coal-burning boiler coal economizer flue-gas temperature between 300~400 DEG C, fire box temperature 850~
Between 1100 DEG C.Traditional SNCR denitration technology reaction temperature window is between 850~1000 DEG C, traditional SCR denitration technology reaction
Temperature window is between 320~410 DEG C, and traditional SNCR+SCR denitration technology is widely used in coal-burning boiler at present, and denitration efficiency is high
Up to 95%, but since coke oven flue gas temperature is relatively low, and coke oven furnace type structure is more special, traditional SNCR, SCR denitration skill
Art is not used to coke oven flue gas denitration improvement.Had developed some low-temperature denitration technologies now, as oxidizing process (oxidant:
Ozone, hydrogen peroxide and sodium hypochlorite etc.) denitration technology and low temperature SCR denitration technology, oxidizing process denitration technology operating cost is high, and
Nitrous oxides concentration is higher in coke oven flue gas, and oxidizing process denitration technology is unsuitable for coke oven flue gas denitration process, it has been developed that SCR
Low temperature catalyst can carry out denitration between 160~300 DEG C, but since low temperature catalyst resistance to SO_2 is excessively poor, low temperature is urged
Agent requires sulfur dioxide concentration≤50mg/Nm3If sulfur dioxide concentration is excessively high, when using SCR denitration technology, catalyst
It can make SO in flue gas2It is oxidized to SO3, SO3It is reacted with the ammonia of penetrating, generates sulfate of ammoniac or hydrogen sulfate ammonia, sulfate of ammoniac and sulfuric acid
Hydrogen ammonia can be attached to catalyst and show that catalyst is caused to lose activity.The formation of sulfate of ammoniac and hydrogen sulfate ammonia is reversible, flue gas
Temperature is higher than 280 DEG C, the sulfate of ammoniac distillation that can make.Flue-gas temperature is higher than 316 DEG C, the hydrogen sulfate ammonia distillation that can make.This
It is the reason of coal-burning boiler tradition SCR denitration requires temperature window to be 320-400 DEG C.
1300 DEG C of coke oven combustion room temperature or so, tar in coke-stove gas high-temperature condition can completely burned, normally
In the case of, tar should not in flue gas or content is very low.Present coal chemical enterprise is likely to result in carbon due to longtime running
Change room and combustion chamber string leak, to will cause, tar content in flue gas is excessively high, tar be to the failure of catalyst it is irreversible, such as
Fruit carbonizing chamber and combustion chamber string leakage will return and generate very huge economic loss to enterprise.
Had some enterprises at present using low temperature SCR denitration technology+Wet Flue Gas Desulfurization Technique, all due to catalyst poisoning and
It ends in failure, although wet desulphurization is more high-efficient than dry method and semi-dry desulphurization, investment and operating cost are very high, simultaneously
A large amount of waste water can be generated, and sulfur dioxide concentration is relatively low in coke oven flue gas, 200~250mg/ of SO 2 from fume concentration
Nm3, wet desulphurization should not be used.Therefore, it studies a kind of suitable for the desulfurization of coke oven flue gas, dedusting and denitrating technique device, tool
There is boundless Social benefit and economic benefit.
Summary of the invention
In view of the foregoing defects the prior art has, the invention proposes a kind of coke oven flue gas semi-dry desulphurization, dedusting and
Low-temperature denitration device and its process.
Coke oven flue gas semi-dry desulphurization, dedusting and low-temperature denitration device of the present invention, including pass through flue successively phase
Coke oven even, semi-dry desulphurization tower, bag filter, SCR reactor, air-introduced machine and chimney, rotary atomizer are installed on half-dried
At the top of method desulfurizing tower, tower bottom unloading valve is installed at semi-dry desulphurization tower the taper bucket, bag filter bottom is equipped with spiral transferring
Machine is sent, is connect by drag conveyor and bucket elevator with grey library, the lower part Hui Ku ash bucket is provided with unloading valve;It further include absorbing
Agent preparation system and ammonia feed system, absorbent preparation system include absorbent powder cabin, spiral metering scale, the work being sequentially connected
Skill water tank, technique water pump, pulping tank, slurry can and slurry feeding pump, rotary atomizer are connect with slurry feeding pump by pipeline;
Ammonia feed system includes ammonia water tank, aqua ammonia pump and ammonium hydroxide evaporation mixer, and ammonia water tank is by aqua ammonia pump and ammonium hydroxide evaporation mixing
Device is connect with SCR reactor inlet flue.
Preferably, low temperature catalyst built in SCR reactor, low temperature catalyst is made of several catalyst modules, several to urge
Agent module is arranged in SCR reactor by steel bracket.
Preferably, the low temperature catalyst uses cellular structure.
Preferably, the flue-gas temperature of the low temperature catalyst processing nitrogen-containing oxide is 120 DEG C~230 DEG C.
The process of coke oven flue gas semi-dry desulphurization of the present invention, dedusting and low-temperature denitration device, including it is as follows
Step:
Step 1: the coke oven flue gas come out from coke oven tail portion is sent into inside desulfurizing tower by flue, and absorbent slurry is by pumping
Squeeze into the rotary atomizer being located at the top of absorption tower;
Step 2: in absorption tower, the absorbent and flue gas for being atomized into fine drop are mixed, in flue gas
SO2Chemical reaction occurs and generates sulfate, the SO in flue gas2It is removed, at the same time, the moisture that absorbent is brought into is steamed rapidly
It sends out and dries, flue-gas temperature decreases;
Step 3: desulfurization reaction product and a small amount of unemployed desulfurization absorbent a part go out from desulfurizing tower bottom cone
Mouth discharge, a part take absorption tower out of with flue gas in the form of dry particulate matter, are collected into high-efficient cloth-bag dust precipitator;
Step 4: the flue gas after desulfurization and dedusting enters low temperature SCR denitration reactor, and flue gas is in low temperature SCR denitration reactor
Interior removing nitrogen oxides, using ammonium hydroxide as reducing agent, ammonium hydroxide is SCR denitration with hot fume heating evaporation in evaporation mixer
Ammonia, ammonia subsequently enters flue and flue gas is sufficiently mixed uniformly, then when by SCR reactor, passes through the work of low temperature catalyst
With denitration reaction occurs, neat stress is obtained after denitration reaction and is discharged into atmosphere by air-introduced machine and chimney.
Preferably, in the step 3, desulfurization absorbent slurries are Ca (OH)2Slurries or Na2CO3Solution, spray drying process
For sulfur removal technology using lime or sodium carbonate as desulfurization absorbent, lime or sodium carbonate add that calcium hydroxide cream is made in water or sodium carbonate is molten
Liquid, calcium hydroxide cream or sodium carbonate liquor are by pumping the atomising device squeezed into absorption tower.
Preferably, in the step 3, after semi-dry desulphurization tower, sulfur dioxide concentration≤20mg/ in coke oven flue gas
Nm3, flue-gas temperature is less than 230 DEG C.
Preferably, in the step 3, after high-efficient cloth-bag dust precipitator 14, dust concentration≤10mg/Nm3, flue gas temperature
≤ 220 DEG C of degree.
Preferably, in the step 4, for semi-dry desulphurization outlet temperature less than 230 DEG C, low-temperature denitration belongs to low-temperature denitration,
Its temperature is 160-230 DEG C, and ammonium sulfate fusing point is 230-280 DEG C, and ammonium sulfate is avoided to adhere to catalyst surface, causes catalyst
Failure.
Preferably, in the step 4, denitrification reducing agent is ammonium hydroxide, and ammonium hydroxide squeezes into ammonia water evaporator mixer by aqua ammonia pump
It is interior, enter SCR reactor through flue, under the action of low temperature catalyst, NO is reduced into N2And H2O。
The beneficial effects of the present invention are: (1) device of the present invention, realizes the temperature range pair at 160-230 DEG C
Coke oven flue gas low-temperature denitration;Investment cost is low, operating cost is low, and desulfurization product has temperature market channel, smoke emissioning pollution object
Concentration enjoys national sewerage preferential policy, has significant Social benefit and economic benefit significant well below national standard;
Application field is wide: can use the low-temperature denitrations, desulfurization and dedusting field such as coke oven, waste incinerator, Industrial Stoves;
(2) process of the present invention, desulfurization, dedusting and denitration efficiency are high;Using rotating spraying semi-dry desulphurization
Technology, non-wastewater discharge, desulfurization slag have stable market channel, thoroughly solve environmental issue;It is much high to discharge flue-gas temperature
In flue gas dew point temperature, discharge is without white haze trailing phenomenon, gypsum that the escaping of ammonia existing for the no ammonia process of desulfurization and calcium method desulfurization generate
The problems such as rain;Before denitration using semi-dry desulphurization+dedusting thoroughly solve sulfur dioxide in flue gas, in flue gas tar to catalyst
Activity influence improves the service life of low temperature catalyst.
Detailed description of the invention
Fig. 1 is structural schematic diagram of the invention.
In figure: 1, coke oven;2, flue;3, semi-dry desulphurization tower;4, rotary atomizer;5, absorbent powder cabin;6, spiral meter
Measure scale;7, technique water tank;8, technique water pump;9, pulping tank;10, slurry can;11, slurry feeding pump;12, tower bottom unloading valve;13,
Drag conveyor;14, bag filter;15, SCR reactor;16, ammonia water tank;17, aqua ammonia pump;18, ammonium hydroxide evaporation mixer;
19, low temperature catalyst;20, air-introduced machine;21, chimney;22, screw conveyor;23, bucket elevator;24, Hui Ku;25, ash is unloaded
Valve.
Specific embodiment
In order to which the object of the invention, technical solution is more clearly understood, below with reference to embodiment, the present invention is made further
It is described in detail.
Embodiment 1:
As shown in Figure 1, coke oven flue gas semi-dry desulphurization of the present invention, dedusting and low-temperature denitration device, the device packet
It includes: coke oven 1, flue 2, semi-dry desulphurization tower 3, rotary atomizer 4, absorbent powder cabin 5, spiral metering scale 6, technique water tank 7, work
Skill water pump 8, pulping tank 9, slurry can 10, slurry feeding pump 11, tower bottom unloading valve 12, drag conveyor 13, bag filter 14,
SCR reactor 15, ammonia water tank 16, aqua ammonia pump 17, ammonium hydroxide evaporation mixer 18, low temperature catalyst 19, air-introduced machine 20, chimney 21,
Screw conveyor 22, bucket elevator 23, grey library 24, unloading valve 25.
In above-mentioned apparatus, coke oven 6, semi-dry desulphurization tower 3, bag filter 14, SCR reactor 15, air-introduced machine 20 and cigarette
Chimney is sequentially connected by flue.Rotary atomizer 4 is installed on 3 top of semi-dry desulphurization tower, pacifies at 3 the taper bucket of semi-dry desulphurization tower
Equipped with tower bottom unloading valve 12,14 bottom of bag filter is equipped with screw conveyor 22, is mentioned by drag conveyor 13 and bucket type
It rises machine 23 to connect with grey library 24, grey 24 lower part ash bucket of library is provided with unloading valve 25.
In above-mentioned apparatus, absorbent preparation system includes: absorbent powder cabin 5, spiral metering scale 6, technique water tank 7, technique
Water pump 8, pulping tank 9, slurry can 10 and slurry feeding pump 11.Rotary atomizer is connect with slurry feeding pump by pipeline, is met
Absorbent slurry needed for desulfurizing tower.
In above-mentioned apparatus, ammonia feed system includes: ammonia water tank 16, aqua ammonia pump 17 and ammonium hydroxide evaporation mixer 18, ammonium hydroxide
Tank 16 is connect by aqua ammonia pump and ammonium hydroxide evaporation mixer with 15 gas approach of SCR reactor.
In above-mentioned apparatus, low temperature catalyst 19 is made of several catalyst modules, and several catalyst modules pass through steel bracket
It is arranged in SCR reactor 15, the flue-gas temperature that this denitrification apparatus can handle nitrogen-containing oxide is 120 DEG C~230 DEG C.Low temperature is urged
Agent uses cellular structure.
Device of the present invention realizes the temperature range at 160-230 DEG C to coke oven flue gas low-temperature denitration;Capital cost
With low, operating cost is low, desulfurization product has temperature market channel, smoke emissioning pollution object concentration well below national standard, enjoys
By national sewerage preferential policy, have significant Social benefit and economic benefit significant;Application field is wide: can use coke oven, rubbish
The low-temperature denitrations such as rubbish incinerator, Industrial Stoves, desulfurization and dedusting field;
Embodiment 2:
The process of coke oven flue gas semi-dry desulphurization of the present invention, dedusting and low-temperature denitration device, including it is as follows
Step:
Step 1: from 1 tail portion of coke oven come out coke oven flue gas by flue 2 be sent into desulfurizing tower inside, absorbent slurry by
Pump squeezes into the rotary atomizer 4 at the top of absorption tower;
Step 2: in absorption tower, the absorbent and flue gas for being atomized into fine drop are mixed, in flue gas
SO2Chemical reaction occurs and generates sulfate, the SO in flue gas2It is removed, at the same time, the moisture that absorbent is brought into is steamed rapidly
It sends out and dries, flue-gas temperature decreases;
Step 3: desulfurization reaction product and a small amount of unemployed desulfurization absorbent a part go out from desulfurizing tower bottom cone
Mouth discharge, a part are taken absorption tower out of with flue gas in the form of dry particulate matter, are collected down into high-efficient cloth-bag dust precipitator 14
Come;
Step 4: the flue gas after desulfurization and dedusting enters low temperature SCR denitration reactor, and flue gas is in low temperature SCR denitration reactor
Interior removing nitrogen oxides, using ammonium hydroxide as reducing agent, ammonium hydroxide is SCR denitration with hot fume heating evaporation in evaporation mixer
Ammonia, ammonia subsequently enters flue 2 and flue gas is sufficiently mixed uniformly, then when by SCR reactor 15, passes through low temperature catalyst 19
Effect denitration reaction occurs, after denitration reaction neat stress is discharged into atmosphere by air-introduced machine 20 and chimney 21.
In the step 3, desulfurization absorbent slurries are CaOH2Slurries or Na2CO3Solution, spray drying process sulfur removal technology
Add water that calcium hydroxide cream or sodium carbonate liquor, calcium hydroxide is made using lime or sodium carbonate as desulfurization absorbent, lime or sodium carbonate
Cream or sodium carbonate liquor are by pumping the atomising device squeezed into absorption tower.
In the step 3, after semi-dry desulphurization tower 3, sulfur dioxide concentration≤20mg/Nm in coke oven flue gas3, cigarette
Temperature degree is less than 230 DEG C.
In the step 3, after high-efficient cloth-bag dust precipitator 14, dust concentration≤10mg/Nm3, flue-gas temperature≤220
℃。
In the step 4, for semi-dry desulphurization outlet temperature less than 230 DEG C, low-temperature denitration belongs to low-temperature denitration, temperature
It is 160-230 DEG C, ammonium sulfate fusing point is 230-280 DEG C, and ammonium sulfate is avoided to adhere to catalyst surface, causes catalyst failure.
In the step 4, denitrification reducing agent is ammonium hydroxide, and ammonium hydroxide is squeezed into ammonia water evaporator mixer by aqua ammonia pump 17, warp
Flue 2 enters SCR reactor 15, and under the action of low temperature catalyst 19, NO is reduced into N2And H2O。
Process of the present invention, desulfurization, dedusting and denitration efficiency are high;Using rotating spraying semi-dry desulphurization skill
Art, non-wastewater discharge, desulfurization slag have stable market channel, thoroughly solve environmental issue;Discharge flue-gas temperature is significantly larger than
Flue gas dew point temperature, discharge is without white haze trailing phenomenon, gypsum rain that the escaping of ammonia existing for the no ammonia process of desulfurization and calcium method desulfurization generate
The problems such as;Thoroughly solve using semi-dry desulphurization+dedusting that sulfur dioxide in flue gas, tar is living to catalyst in flue gas before denitration
Property influence, improve the service life of low temperature catalyst 19.
Embodiment 3:
Assuming that having 5.5 meters of coke ovens, flue gas flow 120000Nm3/ h discharge, flue-gas temperature can reach 270 DEG C, cigarette
Sulfur dioxide concentration 200mg/Nm in gas3, nitrous oxides concentration 800mg/Nm3, dust concentration 40mg/Nm3, moisture content 15%.It is de-
Sulfur absorbing agent is calcium hydroxide, and denitrification reducing agent is 25% ammonium hydroxide.
As shown in Figure 1,270 DEG C of the flue gas come out from coke oven 1 enters semi-dry desulphurization tower 3 by flue 2, it is stored in suction
The lime received in agent powder cabin 5 is sent into pulping tank 9 through spiral metering scale 6, and the process water in technique water tank 7 is sent by technique water pump 8
Enter pulping tank 9, calcium hydroxide cream is made, calcium hydroxide milk flow enters slurry can 10, and calcium hydroxide cream, which is squeezed into be located at by slurry feeding pump 11, to be inhaled
Receive the rotary atomizer 4 in tower.In absorption tower, the absorbent and flue gas for being atomized into fine drop are mixed, with flue gas
In SO2Chemical reaction occurs and generates CaSO3, SO in flue gas2It is removed.Waste residue a part after completing desulphurization reaction is with dry
State form is exported from the cone tower bottom unloading valve 12 of semi-dry desulphurization tower 3 and is discharged, a part of desulfurization reaction product and unutilized
Absorbent take desulfurizing tower out of with flue gas in the form of dry particulate matter, be captured down into bag filter 14, by cloth
The screw conveyor 22 of 14 bottom of bag dust collector is discharged, and is sent into grey library 24 by drag conveyor 13 and bucket elevator 23, ash
Unloading valve 25 is set at bottom storehouse portion cone bucket.After the absorbent of hygrometric state sprays into absorption tower, in one side absorbent and flue gas
Sulfur dioxide chemically reacts;Another aspect flue gas transfers heat to absorbent again and is allowed to continuous drying, at the same time cigarette
Temperature degree decreases.After semi-dry desulphurization tower 3, sulfur dioxide concentration≤20mg/Nm in coke oven flue gas3, flue-gas temperature
Less than 230 DEG C.After high-efficient cloth-bag dust precipitator 14, dust concentration≤10mg/Nm3, flue-gas temperature≤220 DEG C.Through cloth bag
The filtered flue gas of deduster 14 enters SCR reactor 15, built-in cellular formula in SCR reactor 15 through ammonium hydroxide evaporation mixer 18
Low temperature catalyst 19.Ammonium hydroxide is sent into ammonium hydroxide by aqua ammonia pump 17 and evaporates blender 18 by ammonia water tank 16, and ammonium hydroxide is mixed in ammonium hydroxide evaporation
Ammonia is generated in clutch 18, and is sent into reactor in 15 gas approach of SCR reactor, in the effect of low temperature catalyst 19
Under, nitrogen oxides has catalytic reduction reaction with ammonia gas and is removed, and purified flue gas is after air-introduced machine 20 through chimney 21
Discharge.Since flue-gas temperature is up to 220 DEG C, so ammonium hydroxide evaporation is not required to separately set heating device, and since flue gas passes through semidry method
The filtering of desulfurizing tower 3 and bag filter 14, flue gas cleannes are very high, not will cause catalyst abrasion, blocking and poisoning.Institute
With the present embodiment also not set steam soot-blower.
The present embodiment exiting flue gas discharges sulfur dioxide concentration≤20mg/Nm3;Dust concentration≤10mg/Nm3;NOxConcentration
≤100mg/Nm3;Well below special emission limit in " coking chemistry emission of industrial pollutants standard " (GB16171-2012)
Regulation, " 6 atmosphere pollution of table especially discharges limit in " coking chemistry emission of industrial pollutants standard " (GB16171-2012)
Regulation in value ": SO2Concentration of emission≤30mg/Nm3, NOxConcentration of emission≤150mg/Nm3, granular material discharged concentration≤15mg/
Nm3。
The present invention can be widely used in flue gas and need purification device occasion, be particularly suitable for coke oven, waste incinerator, industry
The low-temperature denitrations such as kiln, desulfurization and dedusting field.
The foregoing is merely presently preferred embodiments of the present invention and oneself, not with the present invention for limitation, it is all in essence of the invention
Made impartial modifications, equivalent substitutions and improvements etc., should be included in patent covering scope of the invention within mind and principle.
Claims (10)
1. a kind of coke oven flue gas semi-dry desulphurization, dedusting and low-temperature denitration device, which is characterized in that including by flue (2) according to
Secondary connected coke oven (1), semi-dry desulphurization tower (3), bag filter (14), SCR reactor (15), air-introduced machine (20) and chimney
(21), rotary atomizer (4) is installed at the top of semi-dry desulphurization tower (3), is equipped with tower bottom at semi-dry desulphurization tower (3) the taper bucket
Unloading valve (12), bag filter (14) bottom are equipped with screw conveyor (22), are mentioned by drag conveyor (13) and bucket type
It rises machine (23) to connect with grey library (24), grey library (24) lower part ash bucket is provided with unloading valve (25);It further include absorbent preparation system
With ammonia feed system, absorbent preparation system includes the absorbent powder cabin (5) being sequentially connected, spiral metering scale (6), process water
Case (7), technique water pump (8), pulping tank (9), slurry can (10) and slurry feeding pump (11), rotary atomizer (4) and slurries are defeated
Pump (11) is sent to connect by pipeline;Ammonia feed system includes ammonia water tank (16), aqua ammonia pump (17) and ammonium hydroxide evaporation mixer
(18), ammonia water tank (16) connects by aqua ammonia pump (17) and ammonium hydroxide evaporation mixer (18) and SCR reactor (15) gas approach (2)
It connects.
2. coke oven flue gas semi-dry desulphurization according to claim 1, dedusting and low-temperature denitration device, which is characterized in that SCR
Low temperature catalyst (19) built in reactor (15), low temperature catalyst (19) is made of several catalyst modules, if dry catalyst mould
Block is arranged in SCR reactor (15) by steel bracket.
3. coke oven flue gas semi-dry desulphurization according to claim 2, dedusting and low-temperature denitration device, which is characterized in that institute
Low temperature catalyst (19) are stated using cellular structure.
4. coke oven flue gas semi-dry desulphurization according to claim 3, dedusting and low-temperature denitration device, which is characterized in that institute
The flue-gas temperature for stating low temperature catalyst (19) processing nitrogen-containing oxide is 120 DEG C~230 DEG C.
5. the work of a kind of coke oven flue gas semi-dry desulphurization according to any one of claims 1 to 4, dedusting and low-temperature denitration device
Process, which comprises the steps of:
Step 1: from coke oven (1) tail portion come out coke oven flue gas by flue (2) be sent into desulfurizing tower inside, absorbent slurry by
Pump squeezes into the rotary atomizer (4) at the top of absorption tower;
Step 2: in absorption tower, the absorbent and flue gas for being atomized into fine drop are mixed, with the SO in flue gas2Occur
Chemical reaction generates sulfate, the SO in flue gas2It is removed, at the same time, the moisture that absorbent is brought into is evaporated rapidly and does
Dry, flue-gas temperature decreases;
Step 3: desulfurization reaction product and a small amount of unemployed desulfurization absorbent a part are exported from desulfurizing tower bottom cone and are arranged
Out, a part takes absorption tower out of with flue gas in the form of dry particulate matter, is collected into high-efficient cloth-bag dust precipitator (14);
Step 4: the flue gas after desulfurization and dedusting enters low temperature SCR denitration reactor, and flue gas takes off in low temperature SCR denitration reactor
Denitrification, for SCR denitration using ammonium hydroxide as reducing agent, ammonium hydroxide is ammonia with hot fume heating evaporation in evaporation mixer
Gas, ammonia subsequently enters flue (2) and flue gas is sufficiently mixed uniformly, then when by SCR reactor (15), passes through low temperature catalyst
(19) denitration reaction occurs for effect, obtains neat stress after denitration reaction and is discharged into atmosphere by air-introduced machine (20) and chimney (21).
6. the process of coke oven flue gas semi-dry desulphurization according to claim 5, dedusting and low-temperature denitration device, special
Sign is, in the step 3, desulfurization absorbent slurries are Ca (OH)2Slurries or Na2CO3Solution, spray drying process sulfur removal technology
Add water that calcium hydroxide cream or sodium carbonate liquor, calcium hydroxide is made using lime or sodium carbonate as desulfurization absorbent, lime or sodium carbonate
Cream or sodium carbonate liquor are by pumping the atomising device squeezed into absorption tower.
7. the process of coke oven flue gas semi-dry desulphurization according to claim 6, dedusting and low-temperature denitration device, special
Sign is, in the step 3, after semi-dry desulphurization tower (3), and sulfur dioxide concentration≤20mg/Nm in coke oven flue gas3, cigarette
Temperature degree is less than 230 DEG C.
8. the process of coke oven flue gas semi-dry desulphurization according to claim 6 or 7, dedusting and low-temperature denitration device,
It is characterized in that, in the step 3, after high-efficient cloth-bag dust precipitator (14), dust concentration≤10mg/Nm3, flue-gas temperature
≤220℃。
9. the process of coke oven flue gas semi-dry desulphurization according to claim 5, dedusting and low-temperature denitration device, special
Sign is, in the step 4, for semi-dry desulphurization outlet temperature less than 230 DEG C, low-temperature denitration belongs to low-temperature denitration, and temperature is
160-230 DEG C, ammonium sulfate fusing point is 230-280 DEG C, and ammonium sulfate is avoided to adhere to catalyst surface, causes catalyst failure.
10. the process of coke oven flue gas semi-dry desulphurization according to claim 9, dedusting and low-temperature denitration device,
It is characterized in that, in the step 4, denitrification reducing agent is ammonium hydroxide, and ammonium hydroxide squeezes into ammonia water evaporator mixer by aqua ammonia pump (17)
It is interior, enter SCR reactor (15) through flue (2), under the action of low temperature catalyst (19), NO is reduced into N2And H2O。
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN111821856A (en) * | 2020-07-29 | 2020-10-27 | 湖南萃智环保科技有限公司 | Industrial flue gas denitration method |
CN112807999A (en) * | 2021-01-13 | 2021-05-18 | 沈阳铝镁设计研究院有限公司 | Low-temperature denitration system of aluminum oxide roasting furnace |
CN113332849A (en) * | 2021-06-09 | 2021-09-03 | 江苏三井环保股份有限公司 | Flue gas SDA (serial advanced technology architecture) desulfurization and dust removal method |
-
2018
- 2018-11-22 CN CN201811401019.1A patent/CN109331649A/en not_active Withdrawn
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN111821856A (en) * | 2020-07-29 | 2020-10-27 | 湖南萃智环保科技有限公司 | Industrial flue gas denitration method |
CN112807999A (en) * | 2021-01-13 | 2021-05-18 | 沈阳铝镁设计研究院有限公司 | Low-temperature denitration system of aluminum oxide roasting furnace |
CN113332849A (en) * | 2021-06-09 | 2021-09-03 | 江苏三井环保股份有限公司 | Flue gas SDA (serial advanced technology architecture) desulfurization and dust removal method |
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