CN101168118A - Sintering smoke wet method sulphur removing and dust removing technology - Google Patents

Sintering smoke wet method sulphur removing and dust removing technology Download PDF

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Publication number
CN101168118A
CN101168118A CNA200610117516XA CN200610117516A CN101168118A CN 101168118 A CN101168118 A CN 101168118A CN A200610117516X A CNA200610117516X A CN A200610117516XA CN 200610117516 A CN200610117516 A CN 200610117516A CN 101168118 A CN101168118 A CN 101168118A
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flue gas
dust
sintering
tower
wet method
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CN100534587C (en
Inventor
沈晓林
刘显荣
石洪志
戴尔烈
史国敏
邹义舫
姜敏
刘道清
林瑜
石磊
王如意
蒿自勤
贺秀桂
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BEIJING ZHTD TECHNOLOGY Co
Baoshan Iron and Steel Co Ltd
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BEIJING ZHTD TECHNOLOGY Co
Baoshan Iron and Steel Co Ltd
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Priority to CNB200610117516XA priority Critical patent/CN100534587C/en
Priority to BRPI0718179-5A priority patent/BRPI0718179B1/en
Priority to PCT/CN2007/070951 priority patent/WO2008052465A1/en
Priority to KR1020097010370A priority patent/KR101140748B1/en
Publication of CN101168118A publication Critical patent/CN101168118A/en
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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/16—Sintering; Agglomerating
    • C22B1/20—Sintering; Agglomerating in sintering machines with movable grates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—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
    • B01D53/68—Halogens or halogen compounds
    • 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
    • B01D53/68—Halogens or halogen compounds
    • B01D53/70—Organic halogen compounds
    • 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
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/16—Sintering; Agglomerating
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/02—Working-up flue dust
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2047—Hydrofluoric acid
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Abstract

The invention provides a wet desulfuration and dust-removing technology of sintered flue gas. After the pressure is boosted, the sintered flue gas is firstly processed cooling and defluorination, enabling the HF in the flue gas to be collected by alkaline solution and the temperature of the flue gas to be reduced below 80 DEG C, and then the flue gas enters a highly-effective desulfuration absorption tower. The flue gas is rotatablely punched into a slurry pool with high speed by the function of a rotary current device installed inside a projecting tube arranged inside the tower, and then the flue gas is crushed in the slurry and is fully mixed with the slurry, consequently the process of desulfuration and dust-removing is finished. The pure flue gas after being demisted is discharged from a chimney after being heated by the sintered steam. Above 95% desulfuration efficiency and 99% dust-removing efficiency can be realized by the desulfuration and dust-removing technology. The arrangement of a cooling defluorinated device ensures the hot safety property of the absorption tower and reduces the corrosive degree of the inner tower. The highly-effective desulfuration absorption tower is not provided with a slurry circulation pump, and no moving member is installed inside tower, thereby the contacting effect of gas and liquid is perfect. The reheating method by the sintered steam saves the normal GGH, increases the stability of the systematic operation, and reduces the systematic fabrication cost.

Description

Sintering smoke wet method sulphur removing and dust removing technology
Technical field
The present invention relates to a kind of sintering flue gas desulfurization dust collecting process, particularly a kind of wet method sulphur removing and dust removing technology that is used for the Ferrous Metallurgy sinter fume.
Background technology
At present, sinter fume has become SO in the smelting iron and steel 2Main emission source, and domestic the sintering flue gas desulfurization Study on Technology is belonged to blank substantially, this has become the bottleneck of restriction China steel industry development.
For solving sinter fume SO 2Emission problem, existing countermeasure mainly contains two kinds.
The one, select low-sulphur fuel for use or in raw materials for sintering, add desulfurizing agent to reduce SO 2Discharging, as Chinese patent CN1285415A by in raw materials for sintering, add ammoniation burn in desulfurization.Because additive is inhomogeneous bed of material skewness and combustion zone temperature, concentration field, this method desulfuration efficiency is not high.
The 2nd, sinter fume is carried out desulfurization, flue gas desulfurization technique comprises dry method and wet method.Dry technique has recirculating fluidized bed method, rotary spraying technique, active carbon adsorption, electron beam irradiation method etc.The desulfuration efficiency of recirculating fluidized bed method and rotary spraying technique correspondence is not high, generally 70～85%; And the accessory substance after purifying is calcium sulfite unsettled, that be difficult to utilize, will cause very big place to take as long-term stacking, and can cause secondary pollution.Active carbon adsorption has the application achievement in the iron and steel enterprise of Japan, is provided with sintering flue gas desulfurization, the denitrification apparatus that a cover utilizes charcoal absorption as No. 3 sintering machines of Nagoya steel plant.Though this method can reach 95% desulfurization degree and 40% denitration rate, active carbon costs an arm and a leg, cleaning system and absorbent regeneration system complex, and therefore investment and operating cost are high.Japan Patent JP52051846 discloses a kind of technology of electron beam irradiation method, and this technology can reach desulfurization and the denitration rate more than 80%, but power consumption is very high, and the danger of radiation leakage is arranged.More than several sinter fume dry desulfurizing process, all not obvious to the removal effect of the fine solid particle in the flue gas, and do not possess the corresponding measure that the metal in the sinter fume is reclaimed.
Compare with dry method, the application of sintering smoke wet method sulphur technology is more extensive.Japan Kitakyushu system iron institute in sinter fume, makes SO with the magnesium hydroxide spray solution 2Change magnesium sulfate into, and then it is separated from sintering production process through scrubbing tower.Japan Jing Bin system ammonia-ammonium sulfate method that iron adopts carries out sintering flue gas desulfurization, and this method is to utilize ammonia useless in the oven gas and the SO in the sinter fume 2The sulphur ammonium is reclaimed in reaction.At first use ammonium sulfite solution (concentration is 3%) to absorb SO 2And the generation ammonium bisulfite, again absorption liquid is delivered to the NH in coke-oven plant's absorption coke-stove gas 3, and then form ammonium sulfite, sent back to sintering plant again with the utilization that moves in circles.The sintering plant on ground such as the Chiba of Japan, Shui Dao, Lu Dao, Kobe all adopts limestone-gypsum method.Such process unit is and builds up the seventies in last century, adopts early stage the most traditional limestone-gypsum technology, and the process unit level is relatively backward, and cost and operating cost are all higher.The expert thinks that always external technical matters complexity, economy is relatively poor in the industry, moves inadvisable at home.The form difference on the key equipment of wet desulphurization---absorption tower, desulfuration efficiency, system cost, operating cost and system's operation stability etc. also are not quite similar.At present, comparative maturity is a spray column with the absorption tower of using maximum limestone-gypsum methods in the world, and this kind tower at home and abroad uses on the fired power generating unit more than 300,000 kilowatts in a large number.But different with fire coal boiler fume, there are following characteristics in sinter fume:
(1) SO in the sinter fume 2Concentration is lower (generally at 300～1000mg/Nm 3), its lower limit even lower than the smoke density after the fire coal boiler fume wet desulphurization; And sinter fume amount and SO wherein 2Fluctuation of concentration is bigger, and these characteristics have determined sintering flue gas desulfurization must adopt the desulfur technology of high efficiency, low investment.And spray column gas-liquid mass transfer efficient is general, if will remove the SO of low concentration like this 2, must guarantee that sprayed slurry fully covers on the cross section, absorption tower, even spraying layer surpasses 200% with coverage rate between the layer, Dui Ying liquid-gas ratio (W/G) (generally W/G is 12～20) greatly thus, power consumption is very big, and economy is relatively poor.
(2) compare with fire coal boiler fume, the particle diameter of dust particle is less in the sinter fume, and the share of submicron order dust is higher, and traditional spray column is not high to the dust removal efficiency of this particle size range.
(3) the sinter fume temperature relatively low (85～150 ℃) of coming out from electric cleaner, this makes the heat accumulating type gas-gas heat exchanger (GGH) of spray column front portion flue gas after being purified can't be reheated to more than 80 ℃.And the sinter fume complicated component, this will make script more become to worsening with regard to the working condition of more susceptible to plugging GGH, thereby reduce the availability of system.
(4) sinter fume complicated component according to the difference of sintering deposit, contains tens even the HF gas of hundreds of milligram in every cubic metre of sinter fume.In addition, the content of HCl gas and heavy metal is all higher in the sinter fume, and the dust bonding adsorptivity is strong.These characteristics of sinter fume are had higher requirement to the anti-corrosion anti-scale performance of absorption tower and a whole set of desulphurization system, wastewater treatment etc.
Therefore, consider the particularity of sinter fume, wet desulfurizing process and spray column that will extensive use in power plant desulfurization be indiscriminately imitated on the sintering flue gas desulfurization fully, may not be feasible and uneconomical.
Summary of the invention
The technical problem to be solved in the present invention provides a kind of sintering smoke wet method sulphur removing and dust removing technology, has that sintering flue gas desulfurization efficiency of dust collection height, energy consumption are low, economic operating cost, volume is little, cost is low, characteristics such as reliable, to alleviate SO in the sinter fume 2Discharging influence that ecological environment and health are produced, and alleviate the economic loss and the environmental pressure of enterprise.This technology is applicable to different sinter fume amounts, and can adapt to the variation of the gentle smoke components of sintering cigarette in a big way.
The step of the technical scheme that the present invention solves the problems of the technologies described above comprises:
1) sinter fume that comes out from deduster at first cools off defluorinate after booster fan boosts, and promptly utilizes alkali lye that the HF in the flue gas, HCl gas and bulky grain flue dust are removed substantially, simultaneously by alkali lye and technology evaporation of water with below the cigarette temperature drop to 80 ℃;
2) flue gas enters desulfuration absorbing tower, the SO in the flue gas 2With the alkaline reaction in the absorption tower;
3) flue gas after being purified enters demister and removes drop in the flue gas, is discharged from chimney by heat back more then;
4) gypsum slurries that produces step 2) dewaters through two-stage, and moisture content drops to below 10%.
Be different from fire coal boiler fume,, contain tens even the HF gas of hundreds of milligram in every cubic metre of sinter fume according to the difference of sintering deposit.The HF gas attack is extremely strong, and the hydrofluoric acid that water-soluble back generates can produce serious corrosion to absorption tower inner member and anti-corrosion material, and is especially big to the destructiveness of glass-reinforced plastic material, thereby reduced the desulphurization system reliability of operation.For the safe operation that guarantees the absorption tower, reduce the grade of anti-corrosion material in the tower and, before flue gas enters the absorption tower, earlier it cooled off defluorinate for follow-up desulfurization provides The optimum reaction conditions.In this process, flue gas with from the fresh alkaline reaction of lye tank (vat), can remove HF gas wherein substantially; Alkali lye and technology evaporation of water drop to below 80 ℃ flue-gas temperature simultaneously, for follow-up desulfurization provides The optimum reaction conditions.No matter the absorption tower is any anti-corrosion material as working more than 80 ℃ for a long time, the problem that fatigue of materials is aging, reduce service life all can occur.Therefore the intake air temperature with the absorption tower drops to below 80 ℃, helps the long-term use of absorption tower material, has guaranteed the thermal safety on absorption tower.Because the HCl gas in the flue gas also has high solubility, therefore most HCl is removed when the cooling defluorinate, removes oarse-grained flue dust simultaneously.
Flue gas after the supercooling defluorinate enters the distinctive high-efficiency desulfurization of this technology absorption tower, by with the absorption tower in alkaline reaction, remove SO wherein substantially 2Because the SO in the sinter fume 2Concentration is lower, as adopts traditional spray column form, and then will reach higher desulfuration efficiency need provide very high power consumption.Therefore, the desulfuration absorbing tower of this process using particular design.This absorption tower does not adopt traditional slurries to beat the mode of circulation, top spray, but allowing the flue gas that cools off after fluorine takes off enter equably the some air jet pipes of arranging by certain way in the tower from the middle part, absorption tower, the steam vent of air jet pipe bottom is immersed under the absorbent slurry face.Behind the swirl-flow devices of flue gas in air jet pipe, produce strong rotation, tangentially pour the slurries pond, absorption tower from steam vent subsequently, bubble go out that the back takes place to liquidate mutually, rotates, shearing, fragmentation, in slurries, further smashed, strengthen gas-liquid contact effect, can reach desulfuration efficiency and 99% above efficiency of dust collection more than 95% in this course.Bottom, slurries pond, absorption tower is rabbling mechanism and oxidation unit.The rabbling mechanism purpose is that the gypsum that prevents bottom, slurries pond precipitates; The effect of oxygenation machanism is that byproduct of reaction further is oxidized to available gypsum crystal.When the gypsum slurries concentration of slurries pond, absorption tower bottom reached setting value, gypsum slurries escaped and enter follow-up gypsum dehydration system at the bottom of by tower.
Flue gas after being purified enters demister, and the flue gas after demist reaches good drop separation effect.Flue gas after the demist is discharged from chimney after the heat again.
The gypsum slurries that wherein produces after the desulfurization is through the two-stage dehydration, and moisture content drops to below 10%.
As a kind of improvement of the present invention, sinter fume is cooled off defluorinate, in a cooling defluorinate device, carry out.Can guarantee better like this cigarette temperature promptly is reduced to below 80 ℃, remove the HF gas in the flue gas simultaneously substantially.
As another kind of improvement the of the present invention, the waste water that produces in the cooling defluorinate device directly enters Waste Water Treatment.The waste water that produces in the cooling defluorinate device contains F -, Cl -, contain the flue dust of heavy metal and the calcium sulfite of small part, and wastewater flow rate is little, so directly enter Waste Water Treatment, and no longer enters follow-up desulfurizing tower.Thereby alleviated the chlorion and the heavy metal accumulation effect of desulphurization system greatly, alleviated the chlorine corrosion problem of follow-up equipment, and improved the grade of desulfurization by-product gypsum.
As the other improvement of the present invention, the waste water of discharging from cooling defluorinate device is separated the heavy metal in the waste water by operations such as precipitation, the adjustings of pH value, the heavy metal sewage sludge of oven dry reclaims iron wherein after magnetic separation, the iron after the recovery returns sintering machine head end again and participates in joining the ore deposit.Thereby improved the resource utilization of sintering system.
As another kind of improvement the of the present invention, in step 2) desulfuration absorbing tower in, flue gas after the cooling defluorinate is by the effect of swirl-flow devices in the air jet pipe in the absorption tower, high speed is spun in the slurries pond, flue gas is broken and fully mixing with it in slurries, and gas-liquid is finished desulfurization, dust removal process in efficient contact process.Step 2) the high-efficiency desulfurization absorption tower in does not have slurry circulating pump, so operating cost is low.And air velocity height in the absorption tower, so housing structure is comparatively compact, floor space is little.And the inside movement-less part of desulfuration absorbing tower, no nozzle, thus greatly reduce the obstruction and the fouling tendency on absorption tower, system's operational reliability height, maintenance capacity reduces.
As the other improvement of the present invention, the heating process again of the flue gas after the demist of process step 3) is to realize by the sintering waste heat steam that utilizes native system.The waste heat steam that is about to produce in the central cooler cooling sintering deposit process is introduced the steam smoke re-heater, thereby discharges from chimney after flue-gas temperature is heated to 80 ℃ again.This mode of utilizing the sintering waste heat steam has been cancelled expensive GGH and has been avoided the generation of stopping up again to replace the technology of traditional heat accumulating type gas-gas heat exchanger (GGH), thereby has improved the stability of system's operation and reduced cost of investment.
As for above-mentioned alkali lye, so long as energy and SO 2Solution or slurries that the alkaline matter of reaction is configured to all can use.Desulfurization alkaline matter commonly used is calcium-base absorbing agent such as lime stone and white lime, because of it has price advantage preferably.Other also can use as alkali compounds such as sodium base, magnesium base and ammoniums.
Gypsum in this patent refers to any sulfate of forming after the above-mentioned alkaline matter desulfurization.
Because the present invention has adopted above-mentioned technical scheme, makes it compared with prior art, has following advantage and good effect:
1. can adapt to SO in sinter fume amount, flue-gas temperature and the flue gas 2The requirement of change in concentration wider range, desulfuration efficiency reach more than 95%, and efficiency of dust collection reaches 99%, and especially the dust to submicron order has good removal effect.
2. a cooling defluorinate device is set separately before the absorption tower, time below the cigarette temperature drop to 80 ℃ is removed most of HF gas.This measure is providing on the basis of optimum reaction condition for follow-up desulfurization, has guaranteed the thermal safety on absorption tower, has alleviated the etching problem in the tower effectively, has improved the desulphurization system reliability of operation.
3. in cooling defluorinate device, remove most HCl gas and bulky grain flue dust simultaneously, alleviated the chlorion and the heavy metal accumulation effect of desulphurization system, alleviated the chlorine corrosion problem of follow-up equipment, and improved the grade of desulfurization by-product gypsum.
4. a small amount of waste water that cooling defluorinate device is produced is handled, and has reduced wastewater treatment capacity.Simultaneously the heavy metal in the waste water especially iron is reclaimed and deliver to head and participate in joining the ore deposit, improved the resource utilization of sintering system.
5. compare with traditional spray column, the inner movement-less part in the absorption tower of this process using, no nozzle have reduced the possibility of fouling, equipment operational reliability height, and maintenance capacity reduces greatly.
6. compare with traditional spray column, the absorption tower of this process using does not have slurry circulating pump, so operating cost is low.And air velocity height in the absorption tower, so housing structure is comparatively compact, floor space is little.
7. the absorption tower of this process using, flue gas rotates at a high speed and pours in the slurries pond, and the gas-liquid contact is effective, the desulfurization dust-removing efficiency height.
8. at the characteristics of sinter fume, utilize the hot again mode of sintering waste heat steam, cancelled expensive GGH and avoided the generation of stopping up again, improved the stability of system's operation and reduced cost of investment to replace traditional heat accumulating type gas hot-air heater.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Fig. 2 is a process system sketch of the present invention.
The specific embodiment
By Fig. 1 to Fig. 2 as can be known, the pending sinter fume that comes out from electrostatic precipitator 6 at first after booster fan 7 boosts, enters the cooling defluorinate device 8 that is positioned at desulfuration absorbing tower 9 front portions and carries out the defluorinate cooling.In this stage, behind flue gas and the fresh alkaline reaction that sprays into cooling defluorinate device 8 from limestone slurry liquid bath 14, and the fresh water (FW) that process technology tank 13 sprays into washs, can remove the HF gas in the sinter fume substantially, flue-gas temperature is reduced to below 80 ℃ simultaneously, for follow-up desulfurization provides optimum reaction condition, and guaranteed the thermal safety on absorption tower.Because the HCl gas in the flue gas also has high solubility, therefore most HCl is removed in the cooling defluorinate, removes the bulky grain flue dust simultaneously.
Wherein, the waste water that produces in cooling defluorinate device 8 directly enters Waste Water Treatment 15.The waste water that produces in the cooling defluorinate device 8 contains F -, Cl -, contain the flue dust of heavy metal and the calcium sulfite of small part, and wastewater flow rate is little, so directly enter Waste Water Treatment, and no longer enters follow-up desulfurizing tower.Thereby alleviated the chlorion and the heavy metal accumulation effect of desulphurization system greatly, alleviated the chlorine corrosion problem of follow-up equipment, and improved the grade of desulfurization by-product gypsum.
The waste water of discharging from cooling defluorinate device 8 is separated the heavy metal in the waste water by operations such as precipitation, the adjustings of pH value at Waste Water Treatment 15, the heavy metal sewage sludge of oven dry reclaims iron wherein after magnetic separator 16 magnetic separation, the head that the iron after the recovery returns sintering machine 4 again participates in joining the ore deposit.Thereby improved the resource utilization of sintering system.Remaining heavy metal can further utilize or send outside processing according to circumstances.
Flue gas after 8 coolings of cooling defluorinate device enters the some air jet pipes of arranging according to certain rules in the desulfuration absorbing tower 9 equably, effect by the swirl-flow devices in the air jet pipe, flue gas turns to down motion in the pipe inward turning, and sprays in the alkali lye along the tangential direction of the steam vent of air jet pipe bottom.Because special air jet pipe arrangement mode, the bubble that ejects is produced violent liquidate in slurries, effects such as shearing, eddy flow, fragmentation, thereby produce the gas-liquid two-phase turbulent region of the blending of a height, strong interference, greatly promoted the gas-liquid mass transfer effect.In this course, the SO in the flue gas 2Be dissolved in and carry out the chemical absorbing reaction in the liquid phase, the residual dust in the flue gas also is removed behind contact liq.Bubble in the turbulent region continues tortuous the rising, until breaking on slurries face top, finishes whole flue gas washing process.The air that the calcium sulfite that the reaction back generates blasts by oxidation fan 12 further is oxidized to calcium sulfate in the slurries basin of absorption tower, and crystallization generates gypsum.The agitator 5 of tower bottom moves all the time to prevent the gypsum slurries precipitation.The desulfuration absorbing tower that the present invention relates to also can adopt whole fiberglass (smoke treatment amount hour) or carbon steel inner lining glass fiber reinforced plastic (when the smoke treatment amount is big) to make except that commonly used carbon steel glass inner-lining scale or rubber liner material.Anticorrosion, the good antiscale property superior performance of fiberglass material, and cost is low; The setting of the defluorinate cooling section 8 more thermal safety and the anticorrosion security on fiberglass absorption tower provides reliable guarantee.
Flue gas after the desulfurization carries out gas-liquid separation from entering demister 10 after desulfuration absorbing tower 9 comes out.The flue gas that comes out from demister 10 could enter chimney 1 by air-introduced machine 2 after needing be heated to 80 ℃ steam smoke re-heater 3.The steam smoke re-heater utilizes the waste heat steam that produces in the central cooler cooling sintering deposit process to be used as thermal source again.
The gypsum slurries that flue gas produces at desulfuration absorbing tower 9 and alkaline reaction enters gypsum dehydration system 11 and dewaters through two-stage.Two-stage dehydration is finished by spiral discharge sedimentation centrifuge or hydrocyclone and vacuum belt machine respectively.Because SO in the sinter fume 2Concentration is lower, so gypsum output is not high, for the load that alleviates the gypsum treatment system and be convenient to dehydration, takes intermittently to go out the mode of cream.Promptly pass through the density of densitometer periodic monitor gypsum slurries, when satisfying when the cream requirement, gypsum slurries self-absorption tower bottom takes out pump by gypsum and draws, and be pumped to the calcium plaster liquid bath, and then be pumped into spiral discharge sedimentation centrifuge (or hydrocyclone) through gypsum dehydration and carry out one-level dehydration, the gypsum after one-level dehydration multiviscosisty further is dewatered to moisture content about 10% with vacuum belt machine.
This sintering smoke wet method sulphur removing and dust removing technology is controlled by the DCS collective and distributive type control system.
Hot test device at a sintering flue gas desulfurization: test is taken from certain sintering plant discharging flue gas with flue gas, and temperature is 150 ℃, and flow is 90000m 3/ h amounts to into mark dry state 5.78 ten thousand (N.d.m 3)/h.SO in the flue gas 2Concentration is 300～800mg/Nm 3, HF concentration is 50～90mg/Nm 3, HCl concentration is 80～150mg/Nm 3, dust concentration is 50～120mg/Nm 3The cigarette temperature is reduced to 80 ℃ behind cooling defluorinate device; When former flue gas was 150 ℃, spray limestone slurry liquid measure was 120～250kg/h in the cooling defluorinate device, and cooling water inflow is 2t/h.Cooled smoke enters the absorption tower and reacts, tower diameter 4m, and slurries face height 3.5m, totally 28 of air jet pipes, swirl-flow devices is positioned at the middle part of air jet pipe.Absorbent is the lime stone slurry of 15%wt, and the slurries amount is 250～500kg/h, and the lime stone consumption is 37.6～75.2kg/h.The 20%wt amount of gypsum of discharging is 0.3～0.6m 3/ h.The oxidation air amount is 3m 3/ min, oxidation air pressure head 49kPa.Flue-gas temperature after the desulfurization is 50 ℃, after the two-stage demist in the flue gas water droplet amount of carrying less than 75mg/Nm 3Heat back flue-gas temperature rises to 80～90 ℃ again.
The desulfuration efficiency of above-mentioned desulphurization system reaches more than 95%, and defluorinate and dechlorination efficiency reach more than 95%, and efficiency of dust collection reaches 99%.Discharging the calcium plaster liquid measure is 0.3～0.6m 3/ h, 50%～60%, the moisture content of gypsum is less than 10% after the vacuum belt machine dehydration by the moisture content after the horizontal spiral discharge sedimentation centrifuge dehydration.The gypsum crystal grain diameter that obtains at last is 46～100 μ m.

Claims (7)

1. sintering smoke wet method sulphur removing and dust removing technology is characterized in that may further comprise the steps:
1) sinter fume that comes out from deduster at first cools off defluorinate after booster fan boosts, and promptly utilizes alkali lye that the HF in the flue gas, HCl gas and bulky grain flue dust are removed substantially, simultaneously by alkali lye and technology evaporation of water with below the cigarette temperature drop to 80 ℃;
2) flue gas enters desulfuration absorbing tower, the SO in the flue gas 2With the alkaline reaction in the absorption tower;
3) flue gas after being purified enters demister and removes drop in the flue gas, is discharged from chimney by heat back more then;
1) gypsum slurries that produces step 2) dewaters through two-stage, and moisture content drops to below 10%.
2. sintering smoke wet method sulphur removing and dust removing technology as claimed in claim 1 is characterized in that: the cooling defluorinate process in the step 1) is carried out in a cooling defluorinate device.
3. sintering smoke wet method sulphur removing and dust removing technology as claimed in claim 2 is characterized in that: a small amount of waste water that produces in the cooling defluorinate device directly enters Waste Water Treatment.
4. sintering smoke wet method sulphur removing and dust removing technology as claimed in claim 4, it is characterized in that: the waste water of discharging from cooling defluorinate device is separated the heavy metal in the waste water by operations such as precipitation, the adjustings of pH value, the heavy metal sewage sludge of oven dry reclaims iron wherein after magnetic separation, the iron after the recovery returns sintering machine head end again and participates in joining the ore deposit.
5. sintering smoke wet method sulphur removing and dust removing technology as claimed in claim 1, it is characterized in that: in step 2) desulfuration absorbing tower in, flue gas after the cooling defluorinate is by the effect of swirl-flow devices in the air jet pipe in the absorption tower, high speed is spun in the slurries pond, flue gas is broken and fully mixing with it in slurries, and gas-liquid is finished desulfurization, dust removal process in efficient contact process.
6. sintering smoke wet method sulphur removing and dust removing technology as claimed in claim 1 is characterized in that: the heating again of flue gas utilizes the sintering waste heat steam to realize in the step 3).
7. sintering smoke wet method sulphur removing and dust removing technology as claimed in claim 1 is characterized in that: the alkali lye step 1) and 2) comprises the aqueous solution or the slurries that are configured to by one or more alkali compounds such as lime stone, white lime, sodium base, magnesium base and ammoniums.
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BRPI0718179-5A BRPI0718179B1 (en) 2006-10-25 2007-10-25 WET DESULFURIZATION AND WITHDRAWAL OF SINTERIZATION COMBUSTION GAS DUST.
PCT/CN2007/070951 WO2008052465A1 (en) 2006-10-25 2007-10-25 A sintered flue gas wet desulfurizing and dedusting process
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Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6058230A (en) * 1983-09-09 1985-04-04 Babcock Hitachi Kk Waste gas desulfurization and apparatus thereof
DE3629817A1 (en) * 1986-09-02 1988-03-03 Bergwerksverband Gmbh METHOD FOR REDUCING POLLUTANT EMISSIONS FROM POWER PLANTS WITH COMBINED GAS / STEAM TURBINE PROCESSES WITH UPstream CARBON GASIFICATION
JP2000051648A (en) * 1998-08-05 2000-02-22 Mitsubishi Heavy Ind Ltd Method and apparatus for treating exhaust gas
CN1164352C (en) * 2001-04-23 2004-09-01 崔同顺 Device and process for cleaning tail gas

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