CN1012136B - Method and device for dry purification of flue gas containing mixed harmful components - Google Patents
Method and device for dry purification of flue gas containing mixed harmful componentsInfo
- Publication number
- CN1012136B CN1012136B CN 87108183 CN87108183A CN1012136B CN 1012136 B CN1012136 B CN 1012136B CN 87108183 CN87108183 CN 87108183 CN 87108183 A CN87108183 A CN 87108183A CN 1012136 B CN1012136 B CN 1012136B
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- CN
- China
- Prior art keywords
- dust
- sand
- flue gas
- bed
- gas
- Prior art date
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- 239000003546 flue gas Substances 0.000 title claims abstract description 56
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000000746 purification Methods 0.000 title claims abstract description 27
- 239000000428 dust Substances 0.000 claims abstract description 95
- 239000004576 sand Substances 0.000 claims abstract description 59
- 239000007789 gas Substances 0.000 claims abstract description 34
- 239000002245 particle Substances 0.000 claims abstract description 19
- 239000000843 powder Substances 0.000 claims abstract description 14
- 239000003463 adsorbent Substances 0.000 claims abstract description 13
- 238000001914 filtration Methods 0.000 claims abstract description 11
- 238000009792 diffusion process Methods 0.000 claims abstract description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 61
- 101100041681 Takifugu rubripes sand gene Proteins 0.000 claims description 57
- 239000000292 calcium oxide Substances 0.000 claims description 30
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 30
- 239000000706 filtrate Substances 0.000 claims description 22
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 20
- DLYUQMMRRRQYAE-UHFFFAOYSA-N tetraphosphorus decaoxide Chemical compound O1P(O2)(=O)OP3(=O)OP1(=O)OP2(=O)O3 DLYUQMMRRRQYAE-UHFFFAOYSA-N 0.000 claims description 20
- 238000010521 absorption reaction Methods 0.000 claims description 15
- 239000003517 fume Substances 0.000 claims description 14
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims description 13
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 12
- 230000000505 pernicious effect Effects 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 12
- 239000007787 solid Substances 0.000 claims description 12
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims description 10
- 239000003500 flue dust Substances 0.000 claims description 7
- 239000006004 Quartz sand Substances 0.000 claims description 3
- 210000000498 stratum granulosum Anatomy 0.000 claims 2
- 239000004615 ingredient Substances 0.000 claims 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 abstract description 34
- 239000011737 fluorine Substances 0.000 abstract description 34
- 229910052731 fluorine Inorganic materials 0.000 abstract description 34
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 33
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 14
- 239000011574 phosphorus Substances 0.000 abstract description 14
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 14
- 230000008569 process Effects 0.000 abstract description 12
- 239000000779 smoke Substances 0.000 abstract description 7
- 239000011593 sulfur Substances 0.000 abstract description 7
- 229910052717 sulfur Inorganic materials 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 6
- 238000001179 sorption measurement Methods 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 230000005484 gravity Effects 0.000 abstract description 2
- 239000005864 Sulphur Substances 0.000 description 26
- 238000003723 Smelting Methods 0.000 description 9
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 8
- 229910045601 alloy Inorganic materials 0.000 description 5
- 239000000956 alloy Substances 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 5
- 238000011161 development Methods 0.000 description 4
- 238000005108 dry cleaning Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 229910052761 rare earth metal Inorganic materials 0.000 description 4
- 150000002910 rare earth metals Chemical class 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- 125000004429 atom Chemical group 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000006115 defluorination reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 125000001153 fluoro group Chemical group F* 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 235000010755 mineral Nutrition 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000005453 pelletization Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 229910001021 Ferroalloy Inorganic materials 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 238000005411 Van der Waals force Methods 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000003009 desulfurizing effect 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
- 238000004821 distillation Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005530 etching Methods 0.000 description 1
- 235000013312 flour Nutrition 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000005445 natural material Substances 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
A dry method and a device for purifying flue gas containing mixed harmful gases such as fluorine and the like and dust. The invention is characterized in that a closed smoke collecting hood is adopted to collect smoke and gravity dust removal is carried out; the powder adsorbent is used for turbulent diffusion and adsorption of harmful gas in the conveying bed, cyclone dust removal and filtration purification and dust removal of a cross-flow fluidized bed particle layer (namely a sand filter). The fluorine removal efficiency of the system is more than 99%, the sulfur removal efficiency is more than 92%, and the dust removal efficiency is more than 99%. The sand filter provided by the invention has a simple structure, is easy to manufacture and maintain, not only solves the dust removal problem of phosphorus-containing sticky dust, but also has a deep purification effect on fluorine and sulfur. The invention has simple process flow, high purification and dust removal efficiency, advanced technology, economy and reasonability, and the purified flue gas contains harmful substances such as fluorine, sulfur, phosphorus and the like and dust which accord with the national emission standard.
Description
The present invention relates to a kind of purification method that contains the flue gas that mixes pernicious gas.Be particularly suitable for the dry cleaning method of high temperature viscosity flue gases such as fluorine-containing, sulphur, phosphorus, the invention still further relates to a kind of novel, efficient purifying and dedusting device, be specially adapted to the purification and the dust arrester of high temperature viscosity flue dust.Belong to industrial waste gas treating flour dust technical field.
Development of modern industry particularly contains in processing in the high-temperature smelting process of composition mineral such as fluorine, sulphur, phosphorus, and the fluoride in the mineral, sulfide and phosphide decompose and produce a large amount of hydrogen fluoride (HF), sulfur dioxide (SO of containing
2) and phosphorus pentoxide (P
2O
5) wait the flue gas of pernicious gas and dust, environment has been caused severe contamination.Adopt dry method to carry devices such as bed purification techniques and gravel bed filter thereof, with above-mentioned contaminants matter adsorption cleaning and remove, this is a kind of elimination pernicious gas and dust, improves environment, protection health of human body efficient ways and device.For this reason, seek a kind of adsorbent, design one cover cleaning system and a kind of novel, efficient purifying and dedusting device just becomes the key that realizes this dry cleaning dedusting.
At present, also do not have ripe experience about coloured intermediate alloy flue gases purifications such as electric furnace smelting rare earths both at home and abroad, only some reports are being arranged aspect ferroalloy smelting and the steel-making, but all be limited to collection fume and dust technology.And in the flue gas of coloured intermediate alloys such as electric furnace smelting rare earth except that dust-laden, also contain oxious components such as fluorine, sulphur, phosphorus, this has increased difficulty with regard to the purification techniques of giving flue gas, also need consider the purification of pernicious gas in dedusting.Generally the wet cleaning fluorine of Cai Yonging, the process of sulphur, the flow process complexity, equipment is many, and construction investment is big, and purification efficiency is low, has fouling blocking pipe and etching apparatus, and the secondary pollution problem of fluoride waste is arranged.
The JOY/Niro dry desulfurizing process of the common development of tall dust (JOY) manufacturing company of the U.S. and Denmark Buddhist nun Lip river (Niro) sprayer company (" efforts at environmental protection person's application manual " in November, 1984 that publishing house of Ministry of Metallurgical Industry publishes front page the 244th page) is that to adopt milk of lime, sodium carbonate and ammonia be adsorbent, but its sulfur removal effectiveness has only 90%.
U.S. Pat P3876394 discloses a kind of flue gas that produces from molten aluminium stove, capture through exhaust fume collecting hood, send into fluoride removal system through pipeline and blower fan, quantitatively import fluoride with a kind of alumina powder as adsorbent simultaneously and remove system, in the turbulence air-flow, alumina particle adsorbs to fall fluoride.The flue gas of the above-mentioned processing of process carries out gas solid separation through sack cleaner is again discharged by chimney, and all or part of aluminium smelting furnace that returns of alumina particle that absorption contains fluoride recycles.This technology belongs to the dry method defluorination, and comprehensive reutilization, but the place is this process using that it is not enough is common cyclone dust collectors are removed system as fluoride adsorption reaction equipment, complex structure, in the smoke treatment process, also need introduce outside air and reduce temperature, fluoro-containing concentration in the dilution flue gas, the processing gas flow increases, the energy consumption height, adopt sack cleaner to carry out gas solid separation, non-refractory is unsuitable for handling the flue gas that contains sticky dust, and this technology only can be handled and only contains a kind of single fluoride flue gas.
The object of the present invention is to provide a kind of dry cleaning dust collection method and device of handling high temperature viscosity flue gases such as fluorine-containing, sulphur, phosphorus, technological process is simple, purifying and dedusting efficient height, advanced technology, economical rationality, and flue gas after being purified meets discharging standards.
The present invention realizes like this, the flue gas that electric furnace smelting produced is captured by exhaust fume collecting hood and draws, remove the larger particles dust through gravitational settling, spread with certain speed turbulence in the conveying bed of certain-length with powdered absorbent, pernicious gases such as the fluorine in the absorption flue gas, sulphur are again through cyclone dust collectors and cross-current type thermopnore gravel bed filter, further adsorption cleaning, gas solid separation is removed the CaO dust of fluorine-containing, sulphur, phosphorus and flue dust etc., and flue gas after being purified enters atmosphere through chimney.
Main contents of the present invention are described in detail as follows:
The present invention is that the flue gases that coloured intermediate alloy produced such as electric furnace smelting rare earth are the mixtures of multiple gases, and wherein oxious component mainly contains hydrogen fluoride (HF), sulfur dioxide (SO
2) and phosphorus pentoxide (P
2O
5), its concentration content: HF100～600mg/m
3, SO
2150～1500mg/m
3, P
2O
51.00～5.00mg/m
3Kind of dust 0.18～7.10mg/m
3
One. the purification of pernicious gas such as fluorine-containing, sulphur, phosphorus
1. the purification of fluorine, sulphur:
Flue gas by fire door petticoat pipe and body of heater closed exhaust fume collecting hood capture enters full and uniform contact of powdery calcium oxide adsorbent of carrying bed and adsorbent feeding system to add through gravitational settler, and spreads with the speed turbulence of 17～20m/s.
CaO is to HF, SO
2Catharsis be actually the suction-operated of the surface of solids.When gas molecule in diffusion process during near the surface of solids, the chemical bonding force between the intermolecular Van der Waals force of the surface of solids and surface of solids atom and gas atom makes it produce physical absorption and chemisorbed.CaO is to HF, SO
2Absorption mainly be chemisorbed.In adsorption process, the absorption mass transfer velocity is subjected to the influence of the specific area of diffusion velocity, air film resistance and solid absorbent.Adopt the granule powdery solid to make adsorbent, bigger absorption surface is provided, make it to be in the high turbulence state, improve diffusion velocity, the absorption mass transfer velocity is increased with gas phase.When diffusion velocity and absorption surface one timing, chemisorbed speed depends primarily on the air film resistance.Gas phase is adsorbed matter concentration and increases, and its mass transfer force is also big, and then chemisorbed speeds up.
The CaO content that the present invention uses is greater than 74%, and wherein effective CaO content is greater than 40%, and powder particle size is greater than 200 orders, and wherein 40～60 μ m are greater than 40%.In carrying bed, work as HF concentration at 100～600mg/cm
3, SO
2Concentration is at 150～1500mg/m
3, in the scope, solid-gas ratio 15～60mg/m
3, when flue gas flow rate was 17～20m/s, fluorine removing rate was greater than 97%, and sulfur removal effectiveness is greater than 91%.
Calcium oxide dust and flue gas that absorption contains fluorine, sulphur enter cyclone dust collectors by carrying bed to export, and the CaO that enters cyclone dust collectors still has the ability that continues absorption fluorine, sulphur, and its purification efficiency increases with the increase of its import fluorine, sulphur concentration.Work as inlet concentration: HF1.00～6.00mg/m
3, SO
218.00～90.00mg/m
3The time, the purification efficiency of fluorine is greater than 50%, and the purification efficiency of sulphur is greater than 40%.
Entering cross-current type thermopnore gravel bed filter by the flue gas of cyclone dust collectors outlets is sand filter.Sand filter has the effect of deep purifying to the fluorine in the flue gas, sulphur.This is because filter material surface is wrapped to form similar granule adsorbent by the powdery calcium oxide, also there is calcium oxide between filtrate and the filtrate simultaneously, the filter course of sand filter has become a thermopnore purifier like this, and when flue gas passed through fluidized bed, fluorine, sulphur in the flue gas were further purified.When the sand filter entrance concentration: HF is greater than 8mg/m
3, SO
2Greater than 50mg/m
3, the purification efficiency of fluorine is greater than 92%, and the purification efficiency of sulphur is greater than 80%.
The purification efficiency of whole system fluorine is greater than 99%, and the purification efficiency of sulfur dioxide is greater than 92%.
2. the purification of phosphorus:
Phosphorus pentoxide is a kind of pressed powder of white, distillation in the time of 300 ℃, when flue-gas temperature below 200 ℃ the time, the phosphorus pentoxide major part exists with solid-state form.The flue-gas temperature of exhaust fume collecting hood outlet is 100～210 ℃, phosphorus pentoxide concentration content 1.00～5.00mg/m in the flue gas
3, after carrying bed, cyclone dust collectors and sand filter to purify, the concentration of phosphorus pentoxide is 0.5～1.0mg/m in the sand filter outlet flue gas
3, the purification efficiency of phosphorus can reach 80%.
The flue gas after being purified fluoro-containing concentration is less than 1mg/m
3, contain sulfur dioxide concentration less than 25mg/m
3, contain phosphorus pentoxide concentration less than 1mg/m
3
Two. the purification of system, dust arrester
The history in existing more than 100 year of industrial dedusting device development, early stage deduster is mainly used in recovered material, and efficiency of dust collection is less demanding.Along with industrial expansion, industrial dust is on the rise to the pollution that environment caused, and for the harm of eliminating dust and the strict demand of satisfying environmental protection, thereby has promoted the development of cleaner.According to dust movement rule, various theoretical research and industrial needs of catching dirt mechanism have adopted diversified deduster in production practices.
Deduster commonly used at present has mechanical dust collector, electric cleaner, wet scrubber and filtration dust catcher etc.Filtration dust catcher generally has sack cleaner and gravel bed filter.
With regard to gravel bed filter, at present the most widely used have rake formula or boiling type particle deduster etc., but it also has many defectives, bulky as complex structure, intermittently operated etc.The present invention purifies, dust pelletizing system is a sand filter for the sticky dusts that coloured intermediate alloy produced such as adaptation electric furnace pyrolytic semlting rare earth have designed a kind of cross-current type thermopnore gravel bed filter except that adopting common mechanical gravitational precipitator and cyclone dust collectors.This sand filter dust separation system comprises sand filter, conveying worm, vibration separator and filtrate circulation bucket elevator etc.Sand filter is to have mobile bed that it is divided into inlet plenum and discharge chamber.Mobile bed is by last inferior pyramidal sand hopper, form every sand plate and filtrate, and its thickness of bed layer is 120～145mm.Every the sand plate is detachable frame plate structure, and its air inlet side is that several little deckle boards of 3～5 purpose wire nettings or venetian blind type are formed.The side of giving vent to anger is that several little deckle boards of 10～14 order wire nettings are formed.Entire body is welded by 4～6mm steel plate and angle steel.The optional wide material sources of using of filtrate, low price, high temperature resistant, wear-resisting, corrosion resistant natural material quartz sand, river sand etc., particle diameter of filter medium is 2～5mm.
The present invention has also designed a kind of body of heater closed exhaust fume collecting hood, it is characterized in that this exhaust fume collecting hood adopts flexible skateboard structure (not drawing among the figure) at the electric furnace electrode bus by the sealing of part.The smoke collecting efficiency height of this exhaust fume collecting hood is than the 11000M of open type low hood
3/ h reduces to 3800M
3/ h(is in standard state), pernicious gas components and concentration and dust concentration all are lower than national standard in the smelting shop.
The dust removal process of whole system is:
A large amount of flue gases by exhaust fume collecting hood captures at first enter gravitational settler, and when the gravitational settler resistance is 100～450Pa, the smoke inlet dust concentration is 0.18～7.10g/m
3The time, utilize the gravity natural subsidence, remove the larger particles dust, efficiency of dust collection is greater than 44%.
The flue gas of being drawn by gravitational settler enters carries bed, with powdery calcium oxide adsorbent turbulence diffusion, adsorbs the calcium oxide and the dust of harmful components such as fluorine-containing, sulphur, together enters cyclone dust collectors.When the resistance of cyclone dust collectors is 150～700Pa, the smoke inlet dust concentration is 13.-50.00g/m
3The time, average dust removal efficiency is greater than 82%.
The calcium oxide that contains fluorine, sulphur of being discharged by the cyclone dust collectors ash discharging hole can be recycled, and cycle-index can reach 5 times, and the ratio of new and old calcium oxide is 1: 5.
Contain the phosphorus pentoxide sticky dust and the flue gas of calcium oxide dust such as remainder absorption is fluorine-containing, sulphur enters sand filter by cyclone dust collectors outlets.The efficiency of dust collection of sand filter is relevant with filtration velocity, resistance, filtrate granularity and import dust concentration etc.Efficiency of dust collection reduces with the increase of filtration velocity, increases with resistance, reduces and improves with particle diameter of filter medium.When filtering wind speed is 0.1～0.4m/s, and resistance is 1500～300Pa, and particle diameter of filter medium is 2～5mm, and sand filter inlet plenum section air velocity is less than 1m/s, and dust concentration is less than 20g/m
3In the scope, efficiency of dust collection is 95～99.5%.
Being loaded with the calcium oxide powder of harmful components such as fluorine-containing, sulphur, phosphorus and the filtrate of flue dust is discharged by the sand filter sand export, send into vibration separator through conveying worm and carry out particle separation, remove dust and less than the broken little filtrate of 2mm, the filtrate of particle diameter 2～5mm enters bucket elevator, returns sand filter and recycles.For guaranteeing that the mobile bed of sand filter is full of filtrate, should replenish an amount of fresh sand.
For eliminating the dust that vibration separator and additional fresh sand material are produced, ad hoc meter pipeline and blower fan draw the wind deduster that circles round with it and carry out gas solid separation, to reduce the reentrainment of dust amount.
Advantage of the present invention be to be that adsorbent is carried pernicious gas and dust such as the bed dry cleaning is fluorine-containing, sulphur, phosphorus with the calcium oxide powder, compare with traditional wet method: technological process is short, purifying and dedusting efficient height, construction investment is few, producing cost is low, advanced technology, economical rationality.Sand filter apparatus structure provided by the invention is simple, is easy to make and safeguard, has not only solved the dust removal problem of phosphorous sticky dust, and fluorine, sulphur has all been had the effect of deep purifying.Harmful substance such as fluorine-containing in the flue gas after being purified, sulphur, phosphorus and dust all meet the discharge standard of country.
Below in conjunction with accompanying drawing the present invention is further described.
Description of drawings:
Fig. 1 is the system purification process flow diagram;
Fig. 2 is the sand filter front elevational schematic;
Fig. 3 is a sand filter A-A cutaway view.
As shown in Figure 1, the harmful smokes that coloured intermediate alloy produced such as electric furnace smelting rare earth after being captured by fire door petticoat pipe (1) and body of heater closed exhaust fume collecting hood (2), at first enter gravitational settler (3) and remove the larger particles dust and efflux processing.
After flue gas enters the speed turbulence diffusion absorption of adsorbent powder with 17～20m/s of carrying bed (5) and adsorbent feeding system (4) adding immediately, enter cyclone dust collectors (6), cyclonic separation is removed the calcium oxide dust that major part contains fluorine, sulphur, and flue gas enters the dust pelletizing system of sand filter (7) at last.
Shown in Fig. 2,3, flue gas by cyclone dust collectors (6) outlet, enter inlet plenum (18) from the air inlet (17) of sand filter, filtration velocity with 0.1～0.4m/s passes through thermopnore (20) by the air inlet side every sand plate (19), the translational speed that adds with sand inlet (21) is that 1.5～3.0cm/min, particle diameter are the filtrate contact filtration purification of 2～5mm, flue gas after being purified enters discharge chamber (23) by the side of giving vent to anger every sand plate (22), introduces chimney (9) through exhaust outlet (24) by blower fan (16) [as shown in Figure 1] again and enters atmosphere.Be loaded with the calcium oxide powder of harmful components such as fluorine-containing, sulphur, phosphorus and the filtrate of flue dust, enter conveying worm (10) [as shown in Figure 1] by sand export (25), inputted vibration seperator (11) carries out particle separation again, flue dust and calcium oxide powder enter ash-pit (12) and recycle, broken sand enters broken sand launder (13) and effluxes, be that filtrate enters bucket elevator (8) at last, return sand filter and recycle, and mend an amount of new filter sand (14).
The dust that vibration separator (11) and additional new filter sand (14) are produced draws the wind deduster (6) that circles round by pipeline fan (15) with it and carries out gas solid separation.
Embodiment:
By the flue gas that fire door petticoat pipe (1) and body of heater closed exhaust fume collecting hood (2) capture, the about 3800m of exhaust gas volumn
3/ h, the temperature that exports flue gas from exhaust fume collecting hood (2) is 138 ℃, and pressure is 69Pa, and containing HF concentration is 201.4mg/m
3, SO
2Concentration is 899.8mg/m
3, P
2O
5Concentration is 3.04mg/m
3, solid-gas ratio is 20g/m
3Flue gas at first enters gravitational settler (3), and settler inlet dust concentration is 1.810g/m
3, resistance is 340Pa, the outlet dust concentration is 1.22g/m
3, efficiency of dust collection is 32.6%.
A large amount of flue gases are carried in the bed (5) at 20m with the flow velocity of 18s/m and are told attached dose of turbulence diffusion, the HF in the flue gas, SO with the filtrate calcium oxide
2Be adsorbed Deng pernicious gas, enter cyclone dust collectors (6) subsequently, the entrance flue gas temperature of cyclone dust collectors is 85 ℃, and resistance is 400Pa, and containing HF concentration in the flue gas is 5.84mg/m
3, contain SO
2Concentration is 61.1mg/m
3, contain dust 14.08g/m
3Remove the calcium oxide dust that contains fluorine, sulphur through cyclone dust collectors.95 ℃ of cyclone dust collectors exit gas temperatures, pressure is 2000Pa, containing HF concentration is 0.75mg/m
3, contain SO
2Concentration is 11.57mg/m
3, containing dust concentration is 1.80mg/m
3Fluorine removing rate is 99.63%, and sulfur removal effectiveness is 98.71%, and efficiency of dust collection is 87.2%.
The flue gas that contains the phosphorus pentoxide sticky dust of cyclone dust collectors outlet enters sand filter (7), at the sand filter thickness of bed layer is 120mm, filtrate is a quartz sand, particle diameter is 3～5mm, the filter sand translational speed is 1.5～3.0cm/min, resistance is 2000Pa, and filtration velocity is 0.3m/s, and dust inlet concentration is 4.353g/m in the flue gas
3, exit concentration is 0.106g/m
3, efficiency of dust collection is 97.6%, containing HF concentration in the sand filter outlet flue gas is 0.59mg/m
3, fluorine removing rate is 21.33%; Contain SO
2Concentration is 7.09mg/m
3, sulfur removal effectiveness 38.72%.The total system purification efficiency is: defluorination 99.71%, remove sulfur dioxide 99.21%, and dedusting is more than 99%.
Claims (10)
1, a kind of flue gas purifying method that mixes pernicious gas and dust that contains, it comprises that exhaust fume collecting hood captures flue gas, gravitational dust collection, carry bed absorption, cyclone dust removal and stratum granulosum udst separation etc., the invention is characterized in that with the calcium oxide powder be adsorbent, turbulence diffusion absorption pernicious gas in carrying bed, CaO content is greater than 74% in its powder, effective CaO content is greater than 40%, particle diameter is less than 200 orders, wherein 40-60 μ m is greater than 40%, through cyclone dust removal, cross-current type thermopnore granular bed filter purifying and dedusting, gas solid separation, remove the dust that contains harmful ingredients, flue gas after being purified enters atmosphere.
2, method according to claim 1 is characterized in that wherein said calcium oxide powder can be recycled, cycle-index at least 5 times, and the ratio that fresh CaO and absorption contain the CaO of harmful gas is 1: 5.
3,, it is characterized in that said mixing pernicious gas is hydrogen fluoride (HF), sulfur dioxide (SO according to claim 1,2 described methods
2) and phosphorus pentoxide (P
2O
5) etc., its concentration content: HF is 100～600mg/m
3; SO
2Be 150～1500mg/m
3; P
2O
5Be 1.00～5.00mg/m
3
4, method according to claim 1, it is characterized in that capturing kind of dust is 0.18～7.10g/m
3
5, method according to claim 1 is characterized in that carrying the flue gas flow rate of bed is 17～20m/s.Solid-gas ratio is 15～60g/m
3
6, for realizing the described method of claim 1, full purification dust removal system adopts devices such as exhaust fume collecting hood, gravitational settler, conveying bed, cyclone dust collectors and gravel bed filter.The invention is characterized in the cross-current type thermopnore stratum granulosum dedusting and purifying device system that adopted, this system is by at least one sand filter (7), conveying worm (10), vibration separator (11) and filtrate circulation bucket elevator (8) are formed, sand filter is by mobile bed it to be divided into inlet plenum (18) and discharge chamber (23), flue gas by cyclone dust collectors (6) outlet, enter inlet chamber (18) from the air inlet (17) of sand filter, passing thermopnore (20) by the air inlet side every sand plate (19) purifies with the filtrate contact filtration that sand inlet (21) adds, flue gas after being purified enters discharge chamber (23) by the side of giving vent to anger every sand plate (22), introduce chimney (9) through exhaust outlet (24) by blower fan (6) again and enter atmosphere, be loaded with the calcium oxide powder that contains harmful gas and the filtrate of flue dust, discharge by sand export (25), carry out particle separation through conveying worm (10) inputted vibration seperator (11), calcium oxide powder and flue dust enter ash-pit (12), broken sand enters broken sand launder (13), and filtrate enters bucket elevator (8) and returns sand filter and recycle.
7, device according to claim 6 is characterized in that wherein said mobile bed by last inferior pyramidal sand hopper, form every sand plate and filtrate, and its thickness of bed layer is 120～145mm.
8, according to claim 6,7 described devices, it is characterized in that wherein said is detachable frame plate structure every the sand plate, its air inlet side is that 3～5 order wire nettings or several little deckle boards of venetian blind type are formed, and the side of giving vent to anger is that several little deckle boards of 10-14 order wire netting are formed.
9, according to claim 6,7 described devices, it is characterized in that wherein said filtrate is quartz sand or river sand etc., its particle diameter is 2～5mm.
10, method according to claim 1 is characterized in that the translational speed of filtrate in the bed that flows is 1.5～3.0cm/min, and sand filter inlet plenum section air velocity is less than 1m/s, and sand filter inlet dust concentration is less than 20g/m
3, filtration velocity is 0.1～0.4m/s.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87108183 CN1012136B (en) | 1987-12-15 | 1987-12-15 | Method and device for dry purification of flue gas containing mixed harmful components |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87108183 CN1012136B (en) | 1987-12-15 | 1987-12-15 | Method and device for dry purification of flue gas containing mixed harmful components |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1033508A CN1033508A (en) | 1989-06-28 |
| CN1012136B true CN1012136B (en) | 1991-03-27 |
Family
ID=4816394
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 87108183 Expired CN1012136B (en) | 1987-12-15 | 1987-12-15 | Method and device for dry purification of flue gas containing mixed harmful components |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1012136B (en) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1124368C (en) * | 1999-07-22 | 2003-10-15 | 中国长城铝业公司设计院 | Method for cleaning fluorinated flur gas produced by aluminium electrolysis |
| CN101260322B (en) * | 2006-08-29 | 2011-11-02 | 包头钢铁（集团）有限责任公司 | Blast furnace gas dust removing device and technique by dry method |
| JP4695126B2 (en) * | 2007-09-20 | 2011-06-08 | ジェイパワー・エンテック株式会社 | Desulfurization denitration equipment for exhaust gas |
| CN102179115B (en) * | 2011-05-05 | 2013-05-01 | 无锡市西漳环保设备有限公司 | Smoke dedusting device provided with heating device and used for pouring section and cooling section of resin sand molding |
| US8920540B2 (en) * | 2012-06-08 | 2014-12-30 | Alstom Technology Ltd | Compact air quality control system compartment for aluminium production plant |
| CN102895856B (en) * | 2012-10-31 | 2016-03-09 | 北京清新环境技术股份有限公司 | A kind of equipment of garbage-incineration smoke purifying and process for purifying thereof |
| CN103480224A (en) * | 2013-09-10 | 2014-01-01 | 河南晟道科技有限公司 | High-temperature dust removing system of multilayer ceramic filter material fluidized bed |
| CN104941522B (en) * | 2014-03-31 | 2018-03-30 | 英尼奥斯欧洲股份公司 | Feed distributor for ammonia oxidation reactor designs |
| CN104524893A (en) * | 2014-12-15 | 2015-04-22 | 成都昊特新能源技术股份有限公司 | Process for carrying out combined dust removal on tar-containing flue gas by utilizing dust remover of particle layer of flowing bed and flat-plate membrane filter |
| CN106139792A (en) * | 2015-04-23 | 2016-11-23 | 沈阳铝镁科技有限公司 | A kind of baking flue gas governing system and administering method |
| CN108421413B (en) * | 2018-02-28 | 2020-07-31 | 国家能源投资集团有限责任公司 | Flue gas denitration device and flue gas denitration method |
| MX2022006790A (en) * | 2019-12-03 | 2022-07-11 | 8 Rivers Capital Llc | Direct capture of carbon dioxide. |
| CN116121550B (en) * | 2023-02-22 | 2024-10-01 | 西安聚能高温合金材料科技有限公司 | Automatic dust removal system and dust removal method for protective atmosphere electroslag furnace |
-
1987
- 1987-12-15 CN CN 87108183 patent/CN1012136B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN1033508A (en) | 1989-06-28 |
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