WO2008052465A1 - Procédé de désulfuration et de dépoussiérage par voie humide de gaz de carneau calciné - Google Patents

Procédé de désulfuration et de dépoussiérage par voie humide de gaz de carneau calciné Download PDF

Info

Publication number
WO2008052465A1
WO2008052465A1 PCT/CN2007/070951 CN2007070951W WO2008052465A1 WO 2008052465 A1 WO2008052465 A1 WO 2008052465A1 CN 2007070951 W CN2007070951 W CN 2007070951W WO 2008052465 A1 WO2008052465 A1 WO 2008052465A1
Authority
WO
WIPO (PCT)
Prior art keywords
flue gas
desulfurization
sintering
wet
slurry
Prior art date
Application number
PCT/CN2007/070951
Other languages
English (en)
Chinese (zh)
Inventor
Xiaolin Shen
Hongzhi Shi
Guomin Shi
Daoqing Liu
Yu Lin
Lei Shi
Ruyi Wang
Original Assignee
Baoshan Iron & Steel Co., Ltd.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Baoshan Iron & Steel Co., Ltd. filed Critical Baoshan Iron & Steel Co., Ltd.
Priority to BRPI0718179-5A priority Critical patent/BRPI0718179B1/pt
Priority to KR1020097010370A priority patent/KR101140748B1/ko
Publication of WO2008052465A1 publication Critical patent/WO2008052465A1/fr

Links

Classifications

    • 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

Definitions

  • the invention relates to a sintering flue gas desulfurization and dust removal process, in particular to a wet desulfurization and dust removal process for steel metallurgy sintering flue gas. Background technique
  • the sintering flue gas has become a major iron and steel smelting so 2 emission sources, and domestic research on sintering flue gas desulphurization technology basically blank, which has become a bottleneck restricting the development of China's iron and steel industry.
  • the existing countermeasures are mainly two.
  • low-sulfur fuel is used or a desulfurizing agent is added to the sintering raw material to reduce the emission of so 2.
  • a desulfurizing agent is added to the sintering raw material to reduce the emission of so 2.
  • Chinese patent CN1285415A performs desulfurization in combustion by adding an ammonia-containing compound to the sintering raw material. Due to the uneven distribution of the additive layer and the uneven temperature and concentration field in the combustion zone, the desulfurization efficiency of the method is not high.
  • the second is to desulfurize the sintering flue gas.
  • the flue gas desulfurization technology includes dry and wet methods.
  • the dry process includes a circulating fluidized bed method, a rotary spray method, an activated carbon adsorption method, an electron beam irradiation method, and the like.
  • the desulfurization efficiency corresponding to the circulating fluidized bed method and the rotary spray method is not high, generally 70 ⁇ 85 %; and the by-product after purification is unstable and difficult to use calcium sulfite, such as long-term stacking will cause a large site. Occupied, and will cause secondary pollution.
  • the activated carbon adsorption method has application performance in Japanese steel companies. For example, the No.
  • Japan's Kitakyushu Steel Works sprayed magnesium hydroxide solution into the sintering flue gas to convert S0 2 to magnesium sulfate, which was then separated from the sintering process by a scrubber.
  • Japanese Keihin sintered iron flue gas desulfurization using the ammonia-ammonium sulfate method this method is useless coke oven gas and ammonia sintering reaction S0 2 in the flue gas recovered ammonium sulfate.
  • the S0 2 solution is absorbed by ammonium sulfite solution (concentration: 3%) to form ammonium hydrogen sulfite, and the absorption liquid is sent to the coking plant to absorb NH 3 in the coke oven gas to form ammonium sulfite, which is then sent back to the sintering.
  • Ammonium sulfite solution concentration: 3%) to form ammonium hydrogen sulfite
  • the absorption liquid is sent to the coking plant to absorb NH 3 in the coke oven gas to form ammonium sulfite, which is then sent back to the sintering.
  • Limestone-gypsum method is used in the sinter plants in Chiba, Mizushima, Kashima, and Kobe in Japan. This type of process equipment was built in the 1970s. It adopts the most traditional limestone-gypsum process in the early stage. The level of process equipment is relatively backward, and the cost and operation cost are relatively high. Experts in the industry have always believed that
  • the absorption towers are in different forms, and the desulfurization efficiency, system cost, operating cost, and system operation stability are also different.
  • the limestone-gypsum absorption tower which is relatively mature and widely used in the world, is a spray tower. This type of tower has been widely used in thermal power units of 300,000 kilowatts or more at home and abroad.
  • the sintering flue gas has the following characteristics:
  • the concentration of S0 2 in the sintering flue gas is relatively low (generally 300 ⁇ 1000mg/Nm 3 ), and the lower limit is even lower than that of the flue gas after the wet desulfurization of the coal-fired boiler;
  • the concentration of S0 2 fluctuates greatly.
  • the gas-liquid mass transfer efficiency of the spray tower is generally high. To remove such a low concentration of S0 2 , it is necessary to ensure that the spray slurry is sufficiently covered in the cross section of the absorption tower, and even the coverage between the spray layer and the layer exceeds 200%. Therefore, the corresponding liquid-gas ratio (W/G) is large (generally W/G is 12 to 20), the power consumption is large, and the economy is poor.
  • the temperature of the sintering flue gas from the electrostatic precipitator is relatively low (85 ⁇ 150 °C), which makes the regenerative gas heat exchanger (GGH) at the front of the spray tower unable to remove the purified flue gas. Heat again to above 80 °C.
  • the composition of the sintering flue gas is complicated, which will worsen the working condition of the GGH which is more likely to be blocked, thereby reducing the availability of the system.
  • the composition of the sintering flue gas is complex. Depending on the sinter ore, the sulphur gas per cubic meter contains tens or even hundreds of milligrams of HF gas. In addition, the content of HC1 gas and heavy metals in the sintering flue gas is high, and the dust adsorption and adsorption are strong. These characteristics of the sintering flue gas put forward higher requirements for anti-corrosion and anti-scaling performance of the absorption tower and the whole desulfurization system, and wastewater treatment.
  • the technical problem to be solved by the invention is to provide a wet flue gas desulfurization and dedusting process for sintering flue gas, which has high efficiency of sintering flue gas desulfurization and dust removal, low energy consumption, low operation cost, small volume, low cost, reliable operation, etc.
  • the process is suitable for different sintering flue gas volumes, and can adapt to a wide range of sintering flue gas temperature and smoke composition changes.
  • the sintering flue gas from the precipitator is boosted by the booster fan, it is first cooled and defluorinated, that is, the HF, HC1 gas and large particle soot in the flue gas are basically removed by the alkali solution, and the temperature of the flue is lowered. Up to 80 °C;
  • the purified flue gas enters the mist eliminator to remove droplets from the flue gas, and is then reheated and discharged from the chimney.
  • HF gas is extremely corrosive, and the hydrofluoric acid formed after being dissolved in water will cause serious corrosion to the internal components of the absorption tower and the anticorrosive material, and is particularly destructive to the FRP material, thereby reducing the reliability of the operation of the desulfurization system.
  • the flue gas is cooled and defluorinated before entering the absorption tower.
  • the flue gas reacts with the fresh alkali solution from the lye tank to substantially remove the HF gas therein; at the same time, the evaporation of the lye and the process water reduce the temperature of the flue gas to below 80 ° C for subsequent desulfurization.
  • the intake air temperature of the absorption tower is lowered to below 80 ° C, which is beneficial to the long-term use of the absorption tower material, and ensures the thermal safety of the absorption tower. Since the HC1 gas in the flue gas also has an extremely high solubility, most of the HC1 is removed during cooling defluorination, and large particles of soot are removed.
  • the flue gas after cooling and defluorination enters the high-efficiency desulfurization absorption tower unique to the process, and the S0 2 therein is substantially removed by reacting with the alkali liquid in the absorption tower. Since the concentration of S0 2 in the sintering flue gas is low, as in the case of the conventional spray tower, high power consumption is required to achieve higher desulfurization efficiency. Therefore, this process uses a specially designed desulfurization absorber.
  • the absorption tower does not adopt the traditional slurry circulation cycle and the upper spray method, but allows the flue gas after cooling fluorine to be uniformly transferred from the middle of the absorption tower into a plurality of vent pipes arranged in a certain manner in the tower, the vent tube
  • the lower vent is immersed under the surface of the absorbent slurry.
  • the flue gas passes through the swirling device in the jet tube, it generates a strong rotation, and then rushes from the vent hole into the absorption tower slurry tank.
  • the bubbles are mutually opposed, rotated, sheared and broken after being flushed out, in the slurry. Be further Breaking, enhanced gas-liquid contact effect, in this process can achieve more than 95% desulfurization efficiency and more than 99% of dust removal efficiency.
  • the lower part of the absorption tower slurry tank is a stirring mechanism and an oxidizing device.
  • the purpose of the agitation mechanism is to prevent precipitation of gypsum at the bottom of the slurry tank; the function of the oxidation mechanism is to further oxidize the by-products of the reaction into usable gypsum crystals.
  • concentration of the gypsum slurry at the bottom of the absorption tower slurry tank reaches a set value, the gypsum slurry is discharged from the bottom of the tower and enters a subsequent gypsum dewatering system.
  • the purified flue gas enters the demister, and the flue gas after defogging achieves a good droplet separation effect.
  • the flue gas after the de-fog is reheated and discharged from the chimney.
  • the gypsum slurry produced after desulfurization is subjected to two-stage dehydration, and the water content is reduced to less than 10%, and the two-stage dehydration is respectively performed by a screw discharge sedimentation centrifuge or a hydrocyclone separator and a vacuum belt conveyor. . .
  • the sintering flue gas is cooled and defluorinated, and is carried out in a cooling defluorinator. This will better ensure that the temperature of the smoke is rapidly reduced to below 80 ° C, while substantially removing the HF gas from the flue gas.
  • the temperature of the flue gas in step 1) is cooled by the evaporation of the lye and the process water in the cooled defluorinator.
  • the waste water generated in the cooling defluorinator is directly discharged into the wastewater treatment system.
  • the waste water generated in the cooling defluoridation unit contains F_, Cl_, heavy metal-containing soot and a small amount of calcium sulphite, and the amount of waste water is not large, so it is directly discharged into the wastewater treatment system, and no longer enters the subsequent desulfurization tower.
  • the chloride ion and heavy metal enrichment effects of the desulfurization system are greatly alleviated, the chlorine corrosion problem of the subsequent equipment is alleviated, and the grade of desulfurization by-product gypsum is improved.
  • the waste water discharged from the cooling defluoridation device separates the heavy metal in the waste water by a process such as sedimentation and pH adjustment, and the dried heavy metal sludge is recovered by magnetic separation to recover the iron therein.
  • the iron then returns to the sintering head to participate in the ore blending.
  • the flue gas after cooling and defluorination is passed through the action of the swirling device in the gas injection tube in the absorption tower, and is rapidly swirled into the slurry pool, and the flue gas is The slurry is broken and thoroughly mixed with it, and the gas and liquid complete the desulfurization and dust removal process during the high-efficiency contact process.
  • the high-efficiency desulfurization absorber in step 2) has no slurry circulation pump, so the operating cost is low.
  • the gas flow rate in the absorption tower is high, so the tower body structure is relatively compact and the floor space is small.
  • the reheating process of the flue gas after the demisting by the step 3) is carried out by using the sintering waste heat vapor of the system.
  • the waste heat vapor generated during the cooling and sinter of the ring cooler is introduced into the steam flue gas reheater, so that the flue gas temperature is heated to 80 ° C and then discharged from the chimney.
  • This method of using the residual heat of steam to replace the conventional regenerative gas heat exchanger (GGH) eliminates the expensive GGH and avoids the occurrence of clogging, thereby improving the stability of the system operation and reducing the investment. cost.
  • alkali solution can be used as long as the basic substance the reaction of S0 2 is configured to solution or slurry.
  • desulfurized alkaline materials are calcium-based absorbents such as limestone and slaked lime, which have a good price advantage.
  • Other basic compounds such as sodium, magnesium and ammonium may also be used.
  • the gypsum in this patent refers to any sulfate formed after the above-mentioned alkaline substance is desulfurized.
  • 1 can adapt the amount of sintering gas, flue gas temperature and flue gas so 2 concentration in a wide range of requirements, more than 95% desulfurization efficiency, collection efficiency of 99%, in particular for submicron dust good Remove the effect.
  • the measure ensures the thermal safety of the absorption tower, effectively reduces the corrosion problem in the tower, and improves the reliability of the operation of the desulfurization system.
  • the absorption tower inside the process has no moving parts and no nozzle inside, which reduces the possibility of scale formation, high reliability of equipment operation and greatly reduced maintenance.
  • the absorption tower used in this process has no slurry circulation pump, so the operation cost is low. Moreover, the gas flow rate in the absorption tower is high, so the tower body structure is relatively compact and the floor space is small.
  • Figure 1 is a schematic view of the process flow of the present invention.
  • the sintering flue gas to be treated from the electrostatic precipitator 6 is first pressurized by the turbocharger 7, and then enters the cooling defluoridation unit 8 located at the front of the desulfurization absorption tower 9 for defluorination cooling.
  • the flue gas is reacted with the fresh alkali solution sprayed from the limestone slurry tank 14 into the cooling defluoridation unit 8 and washed by the process water sprayed from the process water tank 13, so that the HF gas in the sintering flue gas can be substantially removed.
  • the temperature of the flue gas is reduced to below 80 ° C, which provides the best reaction conditions for subsequent desulfurization and ensures the thermal safety of the absorption tower. Since the HC1 gas in the flue gas also has an extremely high solubility, most of the HC1 is removed while cooling the defluorination, while removing large particles of soot.
  • the wastewater generated by the cooling defluoridation unit 8 is directly discharged into the wastewater treatment system 15 .
  • the waste water generated in the cooling defluoridation unit 8 contains F_, Cl_, heavy metal-containing soot and a small amount of calcium sulfite, and the amount of waste water is not large, so it is directly discharged into the wastewater treatment system, and no longer enters the subsequent desulfurization tower.
  • the chloride ion and heavy metal enrichment effects of the desulfurization system are greatly reduced, the chlorine corrosion problem of the subsequent equipment is alleviated, and the grade of desulfurization by-product gypsum is improved.
  • the waste water discharged from the cooling defluoridation unit 8 is separated from the heavy metal in the wastewater by a process such as sedimentation and pH adjustment in the wastewater treatment system 15, and the dried heavy metal sludge is magnetically selected by the magnetic separator 16 to recover the iron therein.
  • the recovered iron is returned to the head of the sintering machine 4 to participate in the ore blending. Thereby increasing the resource utilization of the sintering system.
  • the remaining heavy metals may be further utilized or sent out as appropriate.
  • the flue gas cooled from the cooling defluoridation device 8 uniformly enters a plurality of vent pipes arranged in a certain regular pattern in the desulfurization absorption tower 9, and the flue gas rotates downwardly in the tube by the action of the swirling device in the lance tube. It is sprayed into the lye along the tangential direction of the vent hole in the lower part of the lance. Due to the special arrangement of the vent tube, the jetted bubbles produce severe effects such as hedging, shearing, swirling, and crushing in the slurry. Thereby, a gas-liquid two-phase turbulent zone with high mixing and strong interference is generated, which greatly improves the gas-liquid mass transfer effect.
  • So 2 in the flue gas is dissolved in the liquid phase in the process of chemical absorption reaction, after removing the dust remaining in the flue gas are in contact with the liquid.
  • the bubbles in the turbulent zone continue to flicker up until they rupture on the top of the slurry, completing the entire flue gas scrubbing process.
  • the calcium sulfite formed after the reaction is further oxidized into calcium sulfate in the absorption tower slurry storage tank by the air blasted by the oxidation fan 12, and crystallized to form gypsum.
  • the agitator 5 at the bottom of the column is always running to prevent the gypsum slurry from settling.
  • the desulfurization absorption tower of the present invention may also adopt integral FRP (when the amount of flue gas is small) or carbon steel lining FRP (when the amount of flue gas is large) ) to manufacture.
  • FRP material has superior anti-corrosion and anti-fouling performance, and low cost; the defluorination cooling section 8 provides a reliable guarantee for the thermal safety and anti-corrosion safety of the FRP absorption tower.
  • the flue gas after desulfurization exits the desulfurization absorption tower 9 and enters the mist eliminator 10 for gas-liquid separation.
  • the flue gas from the mist eliminator 10 needs to be heated to 80 ° C in the steam flue gas reheater 3 before being discharged into the chimney 1 by the induced draft fan 2 .
  • the steam flue gas reheater uses a ring cooler to cool the waste heat vapor generated during the sintering process as a reheat heat source.
  • the gypsum slurry generated by the reaction of the flue gas in the desulfurization absorption tower 9 and the alkali solution enters the gypsum dehydration system 1 1 and is dehydrated by two stages.
  • the two-stage dewatering is performed by a screw discharge sedimentation centrifuge or a hydrocyclone separator and a vacuum belt conveyor, respectively. Since the concentration of S0 2 in the sintering flue gas is low, the gypsum output is not high.
  • a method of intermittent ointment is adopted. That is, the density of the gypsum slurry is regularly monitored by a densitometer.
  • the gypsum slurry is taken out from the bottom of the absorption tower by a gypsum removal pump, pumped to the gypsum slurry tank, and then sent to the screw discharge by the gypsum dewatering pump.
  • the centrifuge or hydrocyclone performs the first-stage dewatering, and the gypsum thickened by the first-stage dewatering is further dehydrated to a moisture content of about 10% by a vacuum belt conveyor.
  • the wet flue gas desulfurization and dust removal process of the sintering flue gas is controlled by a DCS distributed control system.
  • Test apparatus for a sintering hot flue gas desulfurization test from a sintering plant flue gas discharge flue gas temperature of 150 ° C, flow rate of 90000m 3 / h, converted into dry standard 57800 (N. d. m 3 ) /h.
  • the concentration of S0 2 in the flue gas is 300 ⁇ 800 mg/Nm 3
  • the concentration of HF is 50 ⁇ 90 mg/Nm 3
  • the concentration of HC1 is 80 ⁇ 150 mg/Nm 3
  • the dust concentration is 50 ⁇ 120 mg/Nm 3 .
  • the gas enters the absorption tower for reaction, the diameter of the tower is 4 m, the height of the slurry surface is 3.5 m, and the number of the jet tubes is 28, and the swirling device is located in the middle of the jet tube.
  • the absorbent is 15%wt limestone slurry, the amount of slurry is 250 ⁇ 500kg/h, stone
  • the limestone consumption is 37.6 ⁇ 75.2kg/ho.
  • the amount of 20%wt gypsum discharged is 0.3 ⁇ 0.6 m 3 /h.
  • the amount of oxidizing air was 3 m 3 /min, and the oxidizing air head was 49 kPa.
  • the flue gas temperature after desulfurization is 50 ° C, and the water droplet carrying capacity in the flue gas after two-stage demisting is less than 75 mg/Nm 3 ; the flue gas temperature rises to 80-90 ° C after reheating.
  • the desulfurization efficiency of the above desulfurization system is over 95%, the defluorination and dechlorination efficiency is over 95%, and the dust removal efficiency is 99%.
  • the amount of discharged gypsum slurry is 0.3 ⁇ 0.6 m 3 /h, and the water content after dewatering by the horizontal screw discharge sedimentation centrifuge is 50% ⁇ 60%, and the moisture content of the gypsum after dehydration by the vacuum belt machine is less than 10%.
  • the resulting gypsum crystal particles have a particle size of 46 to 100 ⁇ m.

Abstract

La présente invention concerne un procédé de désulfuration et de dépoussiérage par voie humide de gaz de carneau calciné comprenant : la défluoration du gaz de carneau comprimé avec un alcali et un refroidissement à moins de 80°C, l'introduction du gaz de carneau dans une tour pour la désulfuration et l'absorption (9), la rotation dans un bassin de suspension épaisse (14) par des cyclones dans des conduites de jet de la tour, la floculation du gaz de carneau dans la suspension et le mélange du gaz avec la suspension pour compléter le procédé de désulfuration et de dépoussiérage, la séparation de l'eau du gaz de carneau et le réchauffement par la fumée d'échappement, et la décharge du gaz de carneau épuré depuis une cheminée (1).
PCT/CN2007/070951 2006-10-25 2007-10-25 Procédé de désulfuration et de dépoussiérage par voie humide de gaz de carneau calciné WO2008052465A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
BRPI0718179-5A BRPI0718179B1 (pt) 2006-10-25 2007-10-25 Processo úmido de dessulfurização e retirada de poeiras de gás de combustão de sinterização.
KR1020097010370A KR101140748B1 (ko) 2006-10-25 2007-10-25 습식 소결 연통 가스 탈황 및 탈먼지 공정

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN200610117516.X 2006-10-25
CNB200610117516XA CN100534587C (zh) 2006-10-25 2006-10-25 烧结烟气湿法脱硫除尘工艺

Publications (1)

Publication Number Publication Date
WO2008052465A1 true WO2008052465A1 (fr) 2008-05-08

Family

ID=39343828

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2007/070951 WO2008052465A1 (fr) 2006-10-25 2007-10-25 Procédé de désulfuration et de dépoussiérage par voie humide de gaz de carneau calciné

Country Status (4)

Country Link
KR (1) KR101140748B1 (fr)
CN (1) CN100534587C (fr)
BR (1) BRPI0718179B1 (fr)
WO (1) WO2008052465A1 (fr)

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102580431A (zh) * 2011-04-20 2012-07-18 庄建中 烟气除尘、脱硫一体化工艺
CN102658020A (zh) * 2012-05-24 2012-09-12 首钢总公司 铵-钙双碱法烟气脱硫工艺
CN103990374A (zh) * 2014-05-12 2014-08-20 孙立刚 一种新型燃煤烟气脱硫、脱硝、脱碳、除尘净化联合装置
CN104338423A (zh) * 2013-08-02 2015-02-11 武汉慧邦环境工程技术有限公司 一种用于烟气同时脱硫脱硝的填料塔
CN104479777A (zh) * 2014-11-20 2015-04-01 中国石油大学(北京) 高含硫气体的预处理方法、膜分离方法和系统
CN105833702A (zh) * 2016-05-03 2016-08-10 浙江三龙催化剂有限公司 配套脱硝催化剂隧道窑的除尘设备
CN110841440A (zh) * 2019-12-11 2020-02-28 陕西黑猫焦化股份有限公司 一种焦炉烟气脱硫设备及方法
CN110937579A (zh) * 2019-12-13 2020-03-31 西安润川环保科技有限公司 一种回收废弃脱硫剂的方法
CN111960593A (zh) * 2020-08-04 2020-11-20 中冶北方（大连）工程技术有限公司 活性焦烟气净化制酸废水的处理系统及处理方法
CN112387112A (zh) * 2020-12-03 2021-02-23 北京高能时代环境技术股份有限公司 一种烘干烟气处理系统及方法
CN112456752A (zh) * 2020-11-16 2021-03-09 中国能源建设集团山西省电力勘测设计院有限公司 基于火力发电厂既有设备的污泥直接干化处理方法
CN113019056A (zh) * 2021-03-04 2021-06-25 北京科技大学 一种转轮式烟气脱白装置及工艺
CN113144772A (zh) * 2021-04-30 2021-07-23 青铜峡铝业股份有限公司宁东铝业分公司 一种两段式电解烟气净化排放装置、控制系统及方法
CN113805615A (zh) * 2021-09-09 2021-12-17 井冈山北新建材有限公司 一种自动调节脱硫浆液浓度的系统及方法
CN114053860A (zh) * 2021-11-22 2022-02-18 浙江盈钛斯环保科技有限公司 一种高浓度恶臭气体集成净化处理设备及其处理方法
CN114906965A (zh) * 2022-05-05 2022-08-16 四川永祥股份有限公司 一种废盐回收方法
CN115228242A (zh) * 2022-07-23 2022-10-25 中山市格源环保设备有限公司 一种铝产品喷漆有机废气处理系统及其烟气净化方法
CN115382372A (zh) * 2022-08-23 2022-11-25 河北普阳钢铁有限公司 一种新型焦炉脱硫脱硝节电系统及方法

Families Citing this family (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101549246B (zh) * 2009-04-30 2011-08-17 杭州三和环保技术工程有限公司 烧结烟气脱硫联合焦炉煤气脱氨循环系统
CN101601963B (zh) * 2009-06-02 2012-07-04 张蕊 烟气净化系统及其方法
CN101906328B (zh) * 2009-06-04 2013-07-31 鞍钢集团工程技术有限公司 一种对来自煤粉气化炉荒煤气的净化工艺方法
CN102269527A (zh) * 2010-06-07 2011-12-07 洛阳蓝海实业有限公司 含有脱硫工艺的低温烟气余热利用方法及系统
CN102407066A (zh) * 2010-09-26 2012-04-11 宝山钢铁股份有限公司 烧结烟气湿法脱硝法
CN102000494A (zh) * 2010-12-17 2011-04-06 秦皇岛双轮环保科技有限公司 加镁强化石灰-石膏法烧结机烟气脱硫方法
CN102688667B (zh) * 2012-05-21 2014-10-08 北京中航泰达科技有限公司 移动式集成烟气净化装置
CN102688668B (zh) * 2012-05-21 2014-10-08 北京中航泰达环保科技有限公司 移动式模块化烟气净化装置
JP6107444B2 (ja) * 2013-06-10 2017-04-05 株式会社Ihi 水分含有ガスの不純物除去システム
CN104536371B (zh) * 2014-12-30 2017-02-22 洛阳双瑞万基钛业有限公司 一种电解氯气回收的无人值守自动生产控制方法
GB2540582A (en) * 2015-07-22 2017-01-25 Edwards Ltd Apparatus for evacuating a corrosive effluent gas stream from a processing chamber
CN105091615B (zh) * 2015-08-06 2017-10-31 中南大学 一种铁矿烧结烟气污染物的综合处理方法
CN105540898A (zh) * 2016-02-01 2016-05-04 浙江天地环保工程有限公司 一种超低排放湿式电除尘废水浓缩液处理系统
CN106369623A (zh) * 2016-11-29 2017-02-01 冯伟忠 一种冷凝减排收水加热烘干消除烟羽的系统
CN106693637A (zh) * 2016-12-26 2017-05-24 合肥天翔环境工程有限公司 钢铁冶金中湿法脱硫方法
CN106512611A (zh) * 2016-12-26 2017-03-22 合肥天翔环境工程有限公司 火电厂锅炉烟气脱硫处理方法
CN106621753B (zh) * 2016-12-26 2020-01-24 山东海林环保设备工程有限公司 陶瓷工业窑炉脱硫处理方法
CN106621719A (zh) * 2017-01-19 2017-05-10 北京中航泰达环保科技股份有限公司 含氟烧结/球团烟气处理的方法及系统
CN106621673A (zh) * 2017-01-20 2017-05-10 浙江菲达环保科技股份有限公司 基于低低温的pm2.5团聚装置
CN108499350A (zh) * 2017-02-24 2018-09-07 天津华赛尔传热设备有限公司 一种湿法脱硫的烟气消白系统及方法
CN109745812A (zh) * 2017-11-06 2019-05-14 广州力远环保科技有限公司 一种干、湿法协同治理实现污染物近零排放的技术及装置
CN107638791A (zh) * 2017-11-10 2018-01-30 湖南安普诺环保科技有限公司 一种旋转窑烟气脱硝系统
CN107930376A (zh) * 2017-11-27 2018-04-20 浙江工业大学 一种干湿结合的水泥窑脱硫装置及工艺
CN110787611A (zh) * 2018-08-03 2020-02-14 天津博帆科技发展有限公司 一种热烟气的消白防腐方法
CN109375597A (zh) * 2018-10-23 2019-02-22 国网天津市电力公司电力科学研究院 一种石膏制备智能控制方法
CN111589283A (zh) * 2020-06-24 2020-08-28 上海化工研究院有限公司 一种高效脱除尾气中二氧化硫的方法
CN111701421A (zh) * 2020-06-30 2020-09-25 莱西市济蓝环境生态科技院 一种脱硫方法
CN111701420A (zh) * 2020-06-30 2020-09-25 莱西市济蓝环境生态科技院 一种脱硫设备
KR102301350B1 (ko) * 2020-09-23 2021-09-14 이기호 금속 산 처리시 발생 되는 유독 가스 제거장치 및 그 장치를 이용한 유독 가스 제거 방법
CN113124685B (zh) * 2021-04-19 2022-10-04 中冶长天国际工程有限责任公司 一种烧结源头控制HCl排放的方法和系统
CN113509815B (zh) * 2021-04-19 2022-08-16 中冶长天国际工程有限责任公司 一种烧结烟气多污染物治理中活性炭循环量的调控方法
CN113028836B (zh) * 2021-04-19 2023-12-29 中冶长天国际工程有限责任公司 一种烧结源头控制氯化氢和二氧化硫排放的方法和系统

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4687649A (en) * 1983-09-09 1987-08-18 Babcock-Hitachi Kabushiki Kaisha Flue gas desulfurization process
US4833877A (en) * 1986-09-02 1989-05-30 Bergwerksverband Gmbh Process for the reduction of pollutant emissions from power stations with combined gas/steam turbine processes with preceding coal gasification
JP2000051648A (ja) * 1998-08-05 2000-02-22 Mitsubishi Heavy Ind Ltd 排ガス処理装置及び処理方法

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1164352C (zh) * 2001-04-23 2004-09-01 崔同顺 一种尾气净化处理装置及其该装置完成的工艺

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4687649A (en) * 1983-09-09 1987-08-18 Babcock-Hitachi Kabushiki Kaisha Flue gas desulfurization process
US4833877A (en) * 1986-09-02 1989-05-30 Bergwerksverband Gmbh Process for the reduction of pollutant emissions from power stations with combined gas/steam turbine processes with preceding coal gasification
JP2000051648A (ja) * 1998-08-05 2000-02-22 Mitsubishi Heavy Ind Ltd 排ガス処理装置及び処理方法

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102580431A (zh) * 2011-04-20 2012-07-18 庄建中 烟气除尘、脱硫一体化工艺
CN102580431B (zh) * 2011-04-20 2015-07-22 庄建中 烟气除尘、脱硫一体化工艺
CN102658020A (zh) * 2012-05-24 2012-09-12 首钢总公司 铵-钙双碱法烟气脱硫工艺
CN104338423A (zh) * 2013-08-02 2015-02-11 武汉慧邦环境工程技术有限公司 一种用于烟气同时脱硫脱硝的填料塔
CN103990374A (zh) * 2014-05-12 2014-08-20 孙立刚 一种新型燃煤烟气脱硫、脱硝、脱碳、除尘净化联合装置
CN104479777A (zh) * 2014-11-20 2015-04-01 中国石油大学(北京) 高含硫气体的预处理方法、膜分离方法和系统
CN105833702A (zh) * 2016-05-03 2016-08-10 浙江三龙催化剂有限公司 配套脱硝催化剂隧道窑的除尘设备
CN110841440A (zh) * 2019-12-11 2020-02-28 陕西黑猫焦化股份有限公司 一种焦炉烟气脱硫设备及方法
CN110937579A (zh) * 2019-12-13 2020-03-31 西安润川环保科技有限公司 一种回收废弃脱硫剂的方法
CN111960593A (zh) * 2020-08-04 2020-11-20 中冶北方（大连）工程技术有限公司 活性焦烟气净化制酸废水的处理系统及处理方法
CN112456752A (zh) * 2020-11-16 2021-03-09 中国能源建设集团山西省电力勘测设计院有限公司 基于火力发电厂既有设备的污泥直接干化处理方法
CN112387112A (zh) * 2020-12-03 2021-02-23 北京高能时代环境技术股份有限公司 一种烘干烟气处理系统及方法
CN113019056A (zh) * 2021-03-04 2021-06-25 北京科技大学 一种转轮式烟气脱白装置及工艺
CN113019056B (zh) * 2021-03-04 2022-03-04 北京科技大学 一种转轮式烟气脱白装置及工艺
CN113144772A (zh) * 2021-04-30 2021-07-23 青铜峡铝业股份有限公司宁东铝业分公司 一种两段式电解烟气净化排放装置、控制系统及方法
CN113805615A (zh) * 2021-09-09 2021-12-17 井冈山北新建材有限公司 一种自动调节脱硫浆液浓度的系统及方法
CN113805615B (zh) * 2021-09-09 2023-05-05 井冈山北新建材有限公司 一种自动调节脱硫浆液浓度的系统及方法
CN114053860A (zh) * 2021-11-22 2022-02-18 浙江盈钛斯环保科技有限公司 一种高浓度恶臭气体集成净化处理设备及其处理方法
CN114053860B (zh) * 2021-11-22 2022-06-14 浙江盈钛斯环保科技有限公司 一种高浓度恶臭气体集成净化处理设备及其处理方法
CN114906965A (zh) * 2022-05-05 2022-08-16 四川永祥股份有限公司 一种废盐回收方法
CN115228242A (zh) * 2022-07-23 2022-10-25 中山市格源环保设备有限公司 一种铝产品喷漆有机废气处理系统及其烟气净化方法
CN115228242B (zh) * 2022-07-23 2023-04-11 中山市格源环保设备有限公司 一种铝产品喷漆有机废气处理系统及其烟气净化方法
CN115382372A (zh) * 2022-08-23 2022-11-25 河北普阳钢铁有限公司 一种新型焦炉脱硫脱硝节电系统及方法
CN115382372B (zh) * 2022-08-23 2023-07-18 河北普阳钢铁有限公司 一种新型焦炉脱硫脱硝节电系统及方法

Also Published As

Publication number Publication date
BRPI0718179A2 (pt) 2013-12-17
BRPI0718179B1 (pt) 2018-06-05
CN100534587C (zh) 2009-09-02
KR101140748B1 (ko) 2012-07-12
CN101168118A (zh) 2008-04-30
KR20090112628A (ko) 2009-10-28

Similar Documents

Publication Publication Date Title
WO2008052465A1 (fr) Procédé de désulfuration et de dépoussiérage par voie humide de gaz de carneau calciné
US9895661B2 (en) Process and device for desulphurization and denitration of flue gas
CN100443412C (zh) 酸法焙烧稀土精矿工艺尾气和废水治理方法
WO2019047625A1 (fr) Procédé de commande de production d'aérosol pendant l'absorption dans la désulfuration d'ammoniac
CN103303877B (zh) 多气源低浓度so2烟气综合回收制酸工艺流程
CN105214478A (zh) 一种焦炉烟道废气脱硫脱硝及余热回收的一体化工艺
WO2014172860A1 (fr) Procédé et appareil de traitement de gaz résiduaire acide à l'aide de gaz de combustion par traitement à l'ammoniac
CN102974181A (zh) 一种烟气除尘脱硫脱硝工艺及其专用设备
CN112593034B (zh) 一种高炉净煤气干法协同脱酸系统及方法
CZ291726B6 (cs) Způsob zpracovávání spalin
CN106955571A (zh) 一种工业烟气臭氧分步氧化吸收同时脱硫脱硝的装置及方法
CN103007718B (zh) 一种烟气湿式氧化还原脱硫及资源化利用方法
CN201658945U (zh) 基于热管余热回收技术的烧结烟气净化系统
CN101121096A (zh) 一种燃煤锅炉烟气湿式脱硫除尘工艺
CN103100294A (zh) 臭氧氧化法脱除烟气中氮氧化合物的方法
CN102309920B (zh) 一种脱除FCC烟气中NOx和SOx的方法
CN112225239A (zh) 一种氧化铝生产协同处理钠碱法烟气脱硫废液的方法
CN203108371U (zh) 一种烟气除尘脱硫脱硝工艺的专用设备
CN112619372A (zh) 一种新型煅烧尾气脱硫方法
TW202010565A (zh) 一種氨法脫硫控制吸收過程氣溶膠產生的方法
CN211487169U (zh) 钠碱法脱硫装置
CN109126435B (zh) 一种双碱法烟气脱硫工艺
CN113251420A (zh) 一种工业废弃物的处理方法和装置
CN206266239U (zh) 烟气脱硫剂碳酸氢钠再生装置
CN216935410U (zh) 一种气体脱硫脱氯反应装置和反应系统

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 07817142

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
WWE Wipo information: entry into national phase

Ref document number: 792/MUMNP/2009

Country of ref document: IN

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 1020097010370

Country of ref document: KR

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC, EPO FORM 1205A DATED 20-10-2009.

122 Ep: pct application non-entry in european phase

Ref document number: 07817142

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: PI0718179

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20090427