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WO2012029279A1 - Dispositif de traitement des gaz d'échappement - Google Patents

Dispositif de traitement des gaz d'échappement Download PDF

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Publication number
WO2012029279A1
WO2012029279A1 PCT/JP2011/004794 JP2011004794W WO2012029279A1 WO 2012029279 A1 WO2012029279 A1 WO 2012029279A1 JP 2011004794 W JP2011004794 W JP 2011004794W WO 2012029279 A1 WO2012029279 A1 WO 2012029279A1
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Prior art keywords
exhaust gas
mercury
gas treatment
treatment apparatus
denitration
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Ceased
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PCT/JP2011/004794
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English (en)
Japanese (ja)
Inventor
宍戸　聡
石岡　正明
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Mitsubishi Power Ltd
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Babcock Hitachi KK
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Priority to GB1303447.5A priority Critical patent/GB2498272B/en
Priority to CN2011800408000A priority patent/CN103079692A/zh
Publication of WO2012029279A1 publication Critical patent/WO2012029279A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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
    • B01D53/75—Multi-step processes
    • 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
    • B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
    • 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
    • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
    • 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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
    • B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063—Titanium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/30—Tungsten
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L5/00—Solid fuels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B01D2252/1035—Sea water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20707—Titanium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20776—Tungsten
    • 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
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B01D2257/602—Mercury or mercury compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Definitions

  • the present invention relates to an exhaust gas treatment apparatus, and more particularly, to a technology for removing sulfur oxides in acidic exhaust gas containing mercury generated by coal combustion by absorbing it into seawater.
  • Patent Document 1 acidic exhaust gas containing nitrogen oxides and sulfur oxides generated by coal combustion is introduced into a denitration apparatus, and nitrogen oxides are reduced with a reducing agent such as ammonia in the presence of a catalyst, and denitration is performed.
  • a reducing agent such as ammonia in the presence of a catalyst
  • an exhaust gas treatment apparatus that removes sulfur oxide in acidic exhaust gas discharged from the apparatus by absorbing it in a calcium-based absorption liquid.
  • mercury contained in acidic exhaust gas reacts with halogens such as chlorine contained in the exhaust gas by the catalyst of the denitration device and is converted to mercury oxide. It is described that it is absorbed and removed by the absorbent. Therefore, this document promotes the generation reaction of mercury oxide in the denitration apparatus to remove mercury.
  • Patent Document 2 when a desulfurization apparatus is constructed near the sea, it is proposed to use seawater as an absorbent for the desulfurization apparatus in order to perform desulfurization at a low cost.
  • seawater is sprayed on exhaust gas containing sulfur oxide to absorb the sulfur oxide in the seawater, and then the seawater is neutralized with calcium carbonate and returned to the sea.
  • the problem to be solved by the present invention is to use seawater as the absorbing liquid of the desulfurization apparatus, and to suppress the mercury concentration in the discharged seawater below the allowable value without providing any special waste water treatment.
  • the present invention provides a denitration device for reducing nitrogen oxides in acidic exhaust gas by adding a reducing agent to acidic exhaust gas containing mercury generated by coal combustion, and in the presence of a catalyst,
  • a desulfurization device that absorbs and removes sulfur oxides in acidic exhaust gas discharged from the device into seawater, and the temperature of the acidic exhaust gas on the inlet side of the denitration device suppresses the generation reaction of mercury oxide in the denitration device, and the desulfurization device
  • the mercury oxide concentration at the inlet side is set to a temperature that is lower than the set value.
  • the concentration of mercury oxide in the acidic exhaust gas introduced into the desulfurization device can be controlled and absorbed by seawater that is the absorption liquid of the desulfurization device.
  • the mercury concentration in the released seawater can be kept below the allowable value. Therefore, it is not necessary to perform wastewater treatment to remove mercury from the discharged seawater.
  • the set value of the mercury oxide concentration at the desulfurizer inlet side is appropriately selected according to the allowable value of the mercury concentration in the discharged seawater.
  • the acidic exhaust gas temperature at the inlet side of the denitration device can be set to a temperature at which the mercury concentration in the discharged seawater discharged from the desulfurization device is lower than the set value. That is, an allowable value of mercury concentration in seawater, which is an absorbing liquid discharged from the desulfurization apparatus or circulated to the desulfurization apparatus, is set so that the mercury concentration in the discharged seawater is less than the allowable value (standard value).
  • the acidic exhaust gas temperature at the inlet side of the denitration device is set so that the mercury concentration in the seawater is detected and the allowable value is satisfied.
  • a mercury adsorption device for adsorbing and removing mercury in the acidic exhaust gas on the downstream side of the desulfurization device. According to this, the mercury concentration in the exhaust gas discharged from the exhaust gas treatment device can be reduced.
  • the acidic exhaust gas temperature at the inlet side of the denitration apparatus can be appropriately set according to the allowable value of the mercury concentration in the discharged seawater, and can be set to be 400 ° C. or higher at 100% load, for example. That is, since the generation reaction of mercury oxide in the denitration apparatus is suppressed at a high temperature, it is preferable to increase the temperature of the acidic exhaust gas on the denitration apparatus inlet side. In this case, if the acidic exhaust gas temperature at the inlet side of the denitration device is excessively increased, the denitration rate may be lowered or the heat resistance temperature of the catalyst or the like may be exceeded. Therefore, it is preferable that the acidic exhaust gas temperature at the inlet side of the denitration apparatus is, for example, 450 ° C. or less.
  • the production reaction of mercury oxide in the denitration apparatus is promoted when the chlorine concentration in the acidic exhaust gas is high, it is preferable to burn the coal after washing it with water to reduce the chlorine content in the coal. According to this, since the chlorine concentration in the acidic exhaust gas introduced into the denitration apparatus can be reduced, the generation reaction of mercury oxide can be suppressed.
  • the concentration of mercury in the discharged seawater can be suppressed to an allowable value or less without using seawater as the absorption liquid of the desulfurization apparatus and providing a special waste water treatment.
  • the exhaust gas treatment apparatus 1 of the present embodiment is connected to, for example, a boiler 3 that burns coal, and exhaust gas discharged from the boiler 3, for example, acidic components such as nitrogen oxides and sulfur oxides In addition, exhaust gas containing mercury and mercury is cleaned.
  • the exhaust gas treatment device 1 is provided with a denitration device 7 for denitrating exhaust gas by a selective catalytic reduction method, for example.
  • the denitration device 7 is configured to add a reducing agent 5 such as ammonia to the exhaust gas to reduce nitrogen oxides in the exhaust gas in the presence of a catalyst.
  • a reducing agent 5 such as ammonia
  • an air preheater 9 that heats combustion air of the boiler 3 with exhaust gas is provided.
  • a dust collector 11 that collects particulate matter such as fly ash in the exhaust gas and removes it from the exhaust gas.
  • the desulfurization device 13 is configured to spray seawater pumped by a pump or the like onto the exhaust gas, for example. Thereby, the sulfur oxide in exhaust gas can be absorbed and removed by seawater.
  • the desulfurization device 13 is provided with a purification device (not shown), which removes sulfur oxides absorbed in seawater and discharges the seawater from which sulfur oxides have been removed to the sea.
  • the desulfurization apparatus 13 can be selected as appropriate, such as a circulation type that discharges seawater that is an absorption liquid after circulation, or a one-through type that discharges seawater that has been used once without circulation.
  • a mercury adsorbing device 15 for adsorbing and removing mercury in the exhaust gas is provided on the outlet side of the desulfurization device 13.
  • the mercury adsorption device 15 is provided with, for example, an adsorption tower 17 filled with activated carbon capable of adsorbing mercury and a regeneration tower 19 that removes the mercury adsorbed on the activated carbon and regenerates the activated carbon.
  • a chimney is provided on the outlet side of the mercury adsorption device 15 so as to discharge the purified exhaust gas into the atmosphere.
  • the exhaust gas temperature at the inlet side of the denitration device 7 is set to a temperature at which the detected value or design value of the mercury oxide concentration at the inlet side of the desulfurization device 13 is equal to or less than the set value.
  • the exhaust gas temperature at the inlet side of the denitration device 7 can be set by appropriately adjusting, for example, the heat transfer area of the economizer in the boiler 3 or the amount of water supplied through the boiler 3. Thereby, the exhaust gas temperature at the inlet side of the denitration device 7 is set to a temperature at which the mercury oxide production reaction in the denitration device 7 is suppressed, for example, 400 ° C. or more.
  • the set value of the mercury oxide concentration is appropriately set according to the standard of the allowable limit of the mercury concentration in the discharged seawater of the desulfurization apparatus 13. That is, the mercury concentration in the effluent seawater correlates with the mercury oxide concentration on the inlet side of the desulfurization device 13, and the mercury oxide concentration on the inlet side of the desulfurization device 13 can be adjusted by the exhaust gas temperature on the inlet side of the denitration device 7.
  • the exhaust gas temperature at the inlet side of the denitration device 7 is set so that the mercury oxide concentration at the inlet side is not more than the set value.
  • Nitrogen oxides in the exhaust gas discharged from the boiler 3 are denitrated by the denitration device 7.
  • the denitrated exhaust gas is introduced into the air preheater 9 and reduced in temperature by heat exchange with the combustion air of the boiler 3.
  • the particulate matter such as ash and unburned carbon in the exhaust gas whose temperature has been reduced is removed from the exhaust gas by the dust collector 11.
  • the exhaust gas discharged from the dust collector 11 is sprayed with seawater by the desulfurization device 13, and the sulfur oxide in the exhaust gas is absorbed into the seawater and desulfurized. Seawater that has absorbed sulfur oxides, for example, is discharged into the sea after being purified to remove sulfur oxides.
  • the exhaust gas discharged from the desulfurization device 13 is introduced into the adsorption tower 17 of the mercury adsorption device 15. Thereby, the metallic mercury in the exhaust gas is adsorbed by the adsorbent such as activated carbon and removed from the exhaust gas.
  • the exhaust gas from which mercury has been removed is, for example, heated by a reheater and then released from the chimney 21 into the atmosphere.
  • the exhaust gas temperature on the inlet side of the denitration device 7 is set to a temperature that suppresses the generation reaction of mercury oxide so that the mercury oxide concentration on the inlet side of the desulfurization device 13 is not more than the set value.
  • the mercury oxide concentration in the seawater that is the absorption liquid of the desulfurization device 13 is detected, and the exhaust gas temperature on the inlet side of the denitration device 7 is reduced so that the generation reaction of mercury oxide is suppressed so that the detected value is lower than the set value.
  • Set to the desired temperature That is, an allowable value of mercury concentration in seawater that is an absorption liquid discharged from the desulfurization apparatus 13 or circulated to the desulfurization apparatus 13 is set, and the mercury concentration in seawater as the absorption liquid is less than the allowable value.
  • the exhaust gas temperature on the inlet side of the denitration device 7 can be set. Thereby, since the mercury concentration in the discharged seawater discharged from the desulfurization apparatus 13 can be set to a set value or less, it is not necessary to provide a treatment facility for removing mercury.
  • the exhaust gas temperature on the inlet side of the denitration device 7 can be set to 400 ° C. or higher at 100% load, for example. preferable. If the exhaust gas temperature at the inlet side of the denitration device 7 is excessively high, there is a risk that the NOx removal rate will decrease and the heat resistance temperature of the catalyst or the like may be exceeded. It is preferable to do.
  • Example 1 is an example in which the denitration rate is set to 90% and the exhaust gas temperature at the inlet side of the denitration device 7 is set to 400 ° C. in the denitration device 7 using titanium oxide as a catalyst.
  • Comparative Example 1 is an example in which the exhaust gas temperature on the inlet side of the denitration device 7 is set to 350 ° C. under the conditions of Example 1.
  • Comparative Example 2 is an example in which the exhaust gas temperature at the inlet side of the denitration device 7 is set to 380 ° C.
  • Table 1 shows the results of actual measurement of the mercury oxide production rate in Example 1 and Comparative Examples 1 and 2. Other measurement conditions are as shown in Table 1.
  • Example 1 in which the exhaust gas temperature at the inlet side of the denitration device 7 was set to 400 ° C. can suppress the generation of about 82% mercury oxide compared with Comparative Example 1 set to 350 ° C., and was set to 380 ° C.
  • Comparative Example 2 it was possible to suppress the generation of about 67% mercury oxide. That is, it can be seen that the mercury oxide production reaction correlates with temperature, and that the mercury oxide production reaction can be suppressed as the temperature increases.
  • the production reaction of mercury oxide can be adjusted by the exhaust gas temperature on the inlet side of the denitration device 7 and the concentration of mercury oxide in the exhaust gas introduced into the desulfurization device 13 can be controlled, so that the mercury oxide absorbed in the seawater of the desulfurization device 13 is reduced.
  • the mercury concentration in the released seawater can be made below the allowable value.
  • Example 2 in which a catalyst obtained by adding tungsten as a co-catalyst to titanium oxide was used as Example 2 for the catalyst of Example 1 in which the inlet side exhaust gas temperature of the denitration apparatus 7 was set to 400 ° C. Moreover, the example which burned after performing the water washing process of the coal of Example 2 was made into Example 3.
  • Table 2 shows the results of actual measurement of the mercury oxide production rate (mercury oxidation rate) in Examples 2 to 4. Other measurement conditions are the same as in Example 1.
  • the production reaction of mercury oxide can be further suppressed as compared with Example 1. That is, the exhaust gas temperature at the inlet side of the denitration device 7 is set to 400 ° C., and the catalyst is formed from titanium oxide to which tungsten (W) is added, whereby the generation reaction of mercury oxide can be further suppressed.
  • mercury mercury reacts with mercury metal to produce mercury oxide, as shown in Example 3, it can be burned after the coal is washed with water to reduce the chlorine content in the coal. According to this, the chlorine content in the exhaust gas discharged from the boiler 3 can be reduced, and the production of mercury oxide can be suppressed. Further, when the required denitration rate is, for example, 80% as shown in Example 4, the production reaction of mercury oxide by the catalyst can be suppressed by reducing the amount of catalyst installed in the denitration device 7.
  • the generation reaction of mercury oxide in the desulfurization apparatus 13 can be suppressed and the concentration of mercury oxide in the exhaust gas introduced into the desulfurization apparatus 13 can be reduced, so that it is absorbed by the seawater of the desulfurization apparatus 13.
  • Mercury oxide can be reduced, and the mercury concentration in the discharged seawater can be reduced below the allowable value.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Biomedical Technology (AREA)
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  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
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  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Treating Waste Gases (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Catalysts (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

Le dispositif de traitement des gaz d'échappement est équipé : d'un dispositif de dénitrification (7) destiné à réduire l'oxyde d'azote dans des gaz d'échappement acides par adjonction à ces gaz d'échappement acides à teneur en mercure produits par combustion de charbon, d'un réducteur, en présence d'un catalyseur; et d'un dispositif de désulfuration (13) dans lequel un oxyde de soufre contenu dans les gaz d'échappement acides déchargés par le dispositif de dénitrification (7), est éliminé et absorbé par de l'eau de mer. La température des gaz d'échappement acides côté entrée du dispositif de dénitrification (7), est établie à un niveau selon lequel la réaction de formation d'un oxyde de mercure dans le dispositif de dénitrification (7) est supprimée, et la concentration en oxyde de mercure côté entrée du dispositif de désulfuration (13) est inférieure ou égale à une valeur établie. Par conséquent, la concentration en mercure dans l'eau de mer libérée par le dispositif de désulfuration (13), est inférieure ou égale à une valeur admise.
PCT/JP2011/004794 2010-08-30 2011-08-29 Dispositif de traitement des gaz d'échappement Ceased WO2012029279A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
GB1303447.5A GB2498272B (en) 2010-08-30 2011-08-29 Method for treating acidic exhaust gas containing mercury
CN2011800408000A CN103079692A (zh) 2010-08-30 2011-08-29 废气处理装置

Applications Claiming Priority (2)

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JP2010192295A JP5709438B2 (ja) 2010-08-30 2010-08-30 排ガス処理装置
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JP5991664B2 (ja) * 2012-05-25 2016-09-14 三菱重工環境・化学エンジニアリング株式会社 排煙脱硫システム
EP2724766A1 (fr) * 2012-10-26 2014-04-30 Alstom Technology Ltd Procédé de traitement d'un gaz de combustion riche en dioxyde de carbone et système de traitement de gaz de combustion
TN2019000049A1 (en) * 2016-08-18 2020-07-15 Pacific Green Technologies Inc Integrated wet scrubbing system

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JP2007021442A (ja) * 2005-07-20 2007-02-01 Mitsubishi Heavy Ind Ltd 排ガス処理方法及び設備
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JP2009226238A (ja) * 2008-03-19 2009-10-08 Babcock Hitachi Kk 排ガス処理方法および触媒
WO2010013729A1 (fr) * 2008-07-29 2010-02-04 バブコック日立株式会社 Procédé de purification d'un gaz d'échappement contenant du mercure métallique, catalyseur d'oxydation pour le mercure métallique dans le gaz d'échappement et procédé de fabrication de ce catalyseur

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JP2006205128A (ja) * 2005-01-31 2006-08-10 Babcock Hitachi Kk 排ガス中微量有害物質の除去装置及びその運転方法
JP2007021442A (ja) * 2005-07-20 2007-02-01 Mitsubishi Heavy Ind Ltd 排ガス処理方法及び設備
JP2009226254A (ja) * 2008-03-19 2009-10-08 Chiyoda Kako Kensetsu Kk 水銀吸着材およびその吸着材を用いた排煙処理方法
JP2009226238A (ja) * 2008-03-19 2009-10-08 Babcock Hitachi Kk 排ガス処理方法および触媒
WO2010013729A1 (fr) * 2008-07-29 2010-02-04 バブコック日立株式会社 Procédé de purification d'un gaz d'échappement contenant du mercure métallique, catalyseur d'oxydation pour le mercure métallique dans le gaz d'échappement et procédé de fabrication de ce catalyseur
JP2009208078A (ja) * 2009-06-16 2009-09-17 Mitsubishi Heavy Ind Ltd 排ガス中の水銀処理方法および排ガスの処理システム

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GB2498272A (en) 2013-07-10
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