WO2014129332A1 - 排ガス処理方法、排ガス処理装置、及び、排ガス処理システム - Google Patents
排ガス処理方法、排ガス処理装置、及び、排ガス処理システム Download PDFInfo
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- WO2014129332A1 WO2014129332A1 PCT/JP2014/052968 JP2014052968W WO2014129332A1 WO 2014129332 A1 WO2014129332 A1 WO 2014129332A1 JP 2014052968 W JP2014052968 W JP 2014052968W WO 2014129332 A1 WO2014129332 A1 WO 2014129332A1
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- WIPO (PCT)
- Prior art keywords
- exhaust gas
- gas treatment
- treatment system
- slaked lime
- reaction
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 76
- 239000007789 gas Substances 0.000 claims abstract description 386
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 87
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 87
- 235000011116 calcium hydroxide Nutrition 0.000 claims abstract description 87
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 87
- 238000006243 chemical reaction Methods 0.000 claims abstract description 61
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000011148 porous material Substances 0.000 claims abstract description 25
- 238000000746 purification Methods 0.000 claims abstract description 24
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 23
- 239000003054 catalyst Substances 0.000 claims abstract description 22
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 16
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 14
- 238000004438 BET method Methods 0.000 claims abstract description 11
- 238000003795 desorption Methods 0.000 claims abstract description 11
- 239000002253 acid Substances 0.000 claims description 46
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 18
- 238000003303 reheating Methods 0.000 claims description 5
- 239000012629 purifying agent Substances 0.000 claims 6
- 230000002378 acidificating effect Effects 0.000 abstract description 28
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 24
- 238000006477 desulfuration reaction Methods 0.000 description 16
- 230000023556 desulfurization Effects 0.000 description 16
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 15
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 15
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 15
- 239000000835 fiber Substances 0.000 description 8
- 230000009257 reactivity Effects 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 6
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 5
- 238000010612 desalination reaction Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 5
- 239000004480 active ingredient Substances 0.000 description 4
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 4
- 239000004744 fabric Substances 0.000 description 4
- ZNOKGRXACCSDPY-UHFFFAOYSA-N tungsten trioxide Chemical compound O=[W](=O)=O ZNOKGRXACCSDPY-UHFFFAOYSA-N 0.000 description 4
- 229910052783 alkali metal Inorganic materials 0.000 description 3
- 150000001340 alkali metals Chemical class 0.000 description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 3
- 229910052753 mercury Inorganic materials 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- XHCLAFWTIXFWPH-UHFFFAOYSA-N [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] XHCLAFWTIXFWPH-UHFFFAOYSA-N 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000007872 degassing Methods 0.000 description 2
- 150000002013 dioxins Chemical class 0.000 description 2
- 239000003365 glass fiber Substances 0.000 description 2
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- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000011344 liquid material Substances 0.000 description 2
- 239000010955 niobium Substances 0.000 description 2
- -1 polyfluoroethylene Polymers 0.000 description 2
- 239000010801 sewage sludge Substances 0.000 description 2
- 239000010936 titanium Substances 0.000 description 2
- 229910001935 vanadium oxide Inorganic materials 0.000 description 2
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- 239000004734 Polyphenylene sulfide Substances 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 229910052758 niobium Inorganic materials 0.000 description 1
- GUCVJGMIXFAOAE-UHFFFAOYSA-N niobium atom Chemical compound [Nb] GUCVJGMIXFAOAE-UHFFFAOYSA-N 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 229920000069 polyphenylene sulfide Polymers 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- VSZWPYCFIRKVQL-UHFFFAOYSA-N selanylidenegallium;selenium Chemical compound [Se].[Se]=[Ga].[Se]=[Ga] VSZWPYCFIRKVQL-UHFFFAOYSA-N 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 229910052715 tantalum Inorganic materials 0.000 description 1
- GUVRBAGPIYLISA-UHFFFAOYSA-N tantalum atom Chemical compound [Ta] GUVRBAGPIYLISA-UHFFFAOYSA-N 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000009941 weaving Methods 0.000 description 1
Images
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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Definitions
- the present invention relates to an exhaust gas treatment method, an exhaust gas treatment device, and an exhaust gas treatment system that remove acidic gas in exhaust gas using slaked lime.
- the exhaust gas discharged from a boiler, an incinerator, or the like includes an acidic gas such as hydrogen chloride or sulfur oxide (SO x ). Since acid gas causes air pollution, it is necessary to treat the exhaust gas to remove acid gas.
- FIG. 11 shows an example of an exhaust gas treatment system for treating exhaust gas containing acid gas.
- the exhaust gas treatment system 5 includes a temperature control unit 10 that adjusts the temperature of exhaust gas discharged from the exhaust gas generator A, and slaked lime addition means (gas purification agent addition means) 21 that adds slaked lime (gas purification agent) to the exhaust gas.
- a reaction unit 20 provided, a removal unit 30 for removing the reaction product obtained from the reaction unit 20 from the exhaust gas, a reheater D for reheating the exhaust gas from which the reaction product has been removed, and a denitration treatment for the reheated exhaust gas And a denitration device B.
- the slaked lime addition means 21 adds slaked lime to the exhaust gas, reacts the slaked lime with the acidic gas, and then supplies the slaked lime and the acidic gas to the removal unit 30 through the pipe 22.
- a method of removing the reaction product using a bag filter or the like in the removing unit 30 is widely adopted.
- the acidic gas may condense to produce a liquid acid gas. Since the acidic gas liquid is highly corrosive, it may cause corrosion of the apparatus for treating the exhaust gas.
- the exhaust gas temperature is a high temperature of 220 ° C. or higher, a process for lowering the exhaust gas temperature is required in order to make the temperature of reaction with the acidic gas less than 190 ° C. Therefore, as shown in FIG. 11, the temperature control part 10 which adjusts the temperature of waste gas was provided.
- the present invention relates to an exhaust gas treatment method and exhaust gas treatment that can provide sufficient acid gas removability without increasing the amount of slaked lime, even if the temperature for reacting with acid gas is high (specifically, 190 ° C. or higher).
- An apparatus and an exhaust gas treatment system are provided.
- an exhaust gas treatment method includes a reaction step in which slaked lime is added to an exhaust gas containing an acid gas, and the slaked lime and the acid gas are reacted at 190 ° C. or higher, and the reaction product obtained by the reaction step.
- the slaked lime has a specific surface area measured by the BET method of 25 m 2 / g or more and a pore volume measured by the nitrogen desorption BJH method of 0.15 cm 3 / g or more.
- an exhaust gas purifying catalyst may be supported on the bag filter.
- activated carbon may be added together with slaked lime.
- the exhaust gas treatment device includes gas purification agent addition means for adding a gas purification agent to an exhaust gas of 190 ° C. or higher containing acidic gas, and reacts the gas purification agent with the acidic gas.
- the gas purifier contains slaked lime having a specific surface area measured by the BET method of 25 m 2 / g or more and a pore volume measured by the nitrogen desorption BJH method of 0.15 cm 3 / g or more.
- an exhaust gas purification catalyst may be carried on the bag filter.
- the gas purification agent may further include activated carbon.
- the exhaust gas treatment system includes a gas purification agent adding means for adding a gas purification agent to an exhaust gas of 190 ° C. or higher containing acidic gas, and reacts the gas purification agent with the acidic gas.
- the gas purifier contains slaked lime having a specific surface area measured by the BET method of 25 m 2 / g or more and a pore volume measured by the nitrogen desorption BJH method of 0.15 cm 3 / g or more.
- the exhaust gas treatment system may include a temperature control unit that adjusts the exhaust gas temperature to 190 ° C. or more before the reaction unit.
- a denitration device that denitrates the exhaust gas may be provided after the removal unit.
- a reheater that reheats the exhaust gas may be provided between the removing unit and the denitration apparatus.
- an exhaust gas purification catalyst may be supported on the bag filter.
- the gas purification agent may further include activated carbon.
- exhaust gas treatment method when a bag filter carrying a catalyst for exhaust gas purification is used, dioxins and nitrogen oxides contained in the exhaust gas may be removed. Since it becomes possible, exhaust gas can be further purified. Further, in the exhaust gas treatment method, the exhaust gas treatment apparatus, and the exhaust gas treatment system, when activated carbon is added together with slaked lime, mercury in the exhaust gas can be removed.
- 1 is a schematic diagram showing an exhaust gas treatment device constituting a first embodiment of an exhaust gas treatment system of the present invention. It is a mimetic diagram showing an example of an exhaust gas treatment system of a 1st embodiment. It is a schematic diagram which shows the other example of the waste gas processing system of 1st Embodiment. It is a schematic diagram which shows the exhaust gas processing apparatus which comprises 2nd Embodiment of the exhaust gas processing system of this invention. It is a schematic diagram which shows an example of the exhaust gas processing system of 2nd Embodiment. It is a schematic diagram which shows the other example of the exhaust gas processing system of 2nd Embodiment. It is a graph which shows the desulfurization rate with respect to the specific surface area of slaked lime measured by BET method.
- the exhaust gas treatment system of the present embodiment includes an exhaust gas treatment device 1a shown in FIG.
- the exhaust gas treatment apparatus 1a of the present embodiment is a device that includes a temperature control unit 10, a reaction unit 20, and a removal unit 30, and that processes exhaust gas containing acid gas and removes acid gas from the exhaust gas. .
- Examples of the exhaust gas include gases discharged from various incinerators such as municipal waste incinerators, industrial waste incinerators, sewage sludge incinerators, boilers, diesel engines, and the like.
- Examples of the acidic gas contained in the exhaust gas include hydrogen chloride, sulfur oxide, hydrogen fluoride, and the like.
- the temperature control unit 10 in the present embodiment adjusts the temperature of the exhaust gas containing the acid gas to a temperature suitable for the exhaust gas treatment in a range of 190 ° C. or higher.
- the temperature of the exhaust gas is preferably adjusted by the temperature control unit 10 to be more than 200 ° C. and less than 240 ° C. Further, the temperature of the exhaust gas is more preferably adjusted to 220 ° C. or higher and lower than 240 ° C. Further, the temperature of the exhaust gas is more preferably adjusted to 220 ° C. or more and 235 ° C. or less. If the adjustment temperature of the exhaust gas is lower than 190 ° C., the acidic gas may condense and generate a corrosive liquid material.
- the amount of energy required for heating tends to increase. Since exhaust gas is normally discharged at a high temperature, a cooling device or the like that lowers the exhaust gas temperature is used as the temperature control unit 10. Examples of the cooling device include those using a heat exchanger.
- the reaction unit 20 in this embodiment includes slaked lime addition means 21 that adds slaked lime to exhaust gas.
- the reaction unit 20 reacts slaked lime with the acid gas whose temperature is adjusted to the above range by the temperature control unit 10.
- the slaked lime addition means 21 is connected to the pipe 22 that connects the temperature control unit 10 and the removal unit 30.
- the reaction unit 20 is a part of the pipe 22 between the portion where slaked lime is added by the slaked lime addition means 21 and the removal unit 30.
- reaction with slaked lime and acidic gas arises.
- the slaked lime addition means 21 an existing apparatus or means can be used.
- activated carbon may be added to the exhaust gas together with slaked lime for the purpose of removing mercury in the exhaust gas.
- Slaked lime used in the present embodiment is a particle containing Ca (OH) 2 as a main component.
- This slaked lime has a specific surface area measured by the BET method (hereinafter referred to as “BET specific surface area”) of 25 m 2 / g or more and a pore volume measured by the nitrogen desorption BJH method (hereinafter referred to as “pore volume”). .) Is 0.15 cm 3 / g or more. Even when the BET specific surface area is less than the lower limit (25 m 2 / g) or the pore volume is less than the lower limit (0.15 cm 3 / g), the reactivity to acidic gas at 190 ° C. or higher. Decreases.
- the BET specific surface area of slaked lime is preferably 60 m 2 / g or less.
- the pore volume is preferably 0.3 cm 3 / g or less.
- the BET specific surface area is a value obtained by measuring by adsorbing nitrogen at 77K after degassing slaked lime.
- the pore volume is a value obtained by measuring by degassing slaked lime, adsorbing nitrogen at 77 K, and desorbing nitrogen.
- the BET specific surface area and pore volume can be measured with a commercially available measuring device. Examples of the measuring device include a specific surface area / pore distribution measuring device ASAP series manufactured by Micromeritics.
- the slaked lime may contain an alkali metal in the range of 0.2 to 3.5% by mass.
- the alkali metal include sodium, potassium, and lithium.
- the average particle size of slaked lime is preferably 5 to 12 ⁇ m.
- the average particle size of slaked lime is more preferably 7 to 10 ⁇ m.
- the average particle diameter is a value measured by a laser particle size measuring device or SEM observation.
- the removal unit 30 in the present embodiment includes a bag filter that removes the reaction product obtained by the reaction unit 20 from the exhaust gas.
- the exhaust gas containing the reaction product is supplied to the bag filter, and the reaction product is captured by the bag filter. Thereby, the acid gas content of the exhaust gas that has passed through the bag filter is reduced.
- the reaction product captured by the bag filter is periodically removed and removed from the removal unit 30.
- the bag filter used in the removing unit 30 is a so-called “filter cloth”.
- the filter cloth is formed from a cloth woven by a weaving method such as twill weave, satin weave, or plain weave.
- the driving density of the cloth is preferably 600 to 1200 g / m 2 .
- the driving density is not less than the lower limit (600 g / m 2 )
- the reaction product can be sufficiently captured.
- the driving density is not more than the upper limit (1200 g / m 2 )
- the fibers constituting the bag filter include glass fibers, polyfluoroethylene fibers, polyester fibers, polyamide fibers, polyphenylene sulfide fibers, and the like.
- the fibers glass fibers and polyfluoroethylene fibers are preferable in terms of high heat resistance.
- the fiber diameter is preferably 3 to 15 ⁇ m.
- an exhaust gas purifying catalyst is supported on the bag filter.
- the exhaust gas can be further purified. If the exhaust gas-purifying catalyst carried on the bag filter has nitrogen oxide decomposability, the nitrogen oxide content in the exhaust gas becomes low, and denitration treatment other than the bag filter can be omitted. If the exhaust gas purifying catalyst carried on the bag filter has dioxin decomposability, the dioxin content in the exhaust gas will be low. In general, the higher the temperature, the lower the dioxin removability. However, if the exhaust gas purifying catalyst having dioxin decomposability is supported on the bag filter, even if the temperature is 190 ° C. or higher, the same dioxin removability as that at a temperature lower than 190 ° C. can be obtained.
- the exhaust gas-purifying catalyst carried on the bag filter is a catalyst composed of a carrier composed of a single or complex oxide and an active component composed of an oxide.
- the carrier contains at least one element selected from titanium (Ti), silicon (Si), aluminum (Al), zirconium (Zr), phosphorus (P), and boron (B).
- the active component includes at least one of oxides of vanadium (V), tungsten (W), molybdenum (Mo), niobium (Nb), and tantalum (Ta). It is preferable to use at least titanium oxide as the carrier. It is preferable to use at least vanadium oxide as the active ingredient. All of the above active ingredients have an oxidizing ability and can oxidatively decompose dioxins. Any of the above active ingredients can reduce nitrogen oxides in the presence of a reducing agent. Among the above active ingredients, vanadium oxides are particularly excellent in their ability.
- the composition of the exhaust gas purifying catalyst is not particularly limited.
- the active component is one component of vanadium pentoxide
- the amount is preferably 1 to 20 parts by mass with respect to 100 parts by mass of the carrier.
- the active component is two components of vanadium pentoxide and tungsten trioxide, 1 to 10 parts by mass of vanadium pentoxide and 2 to 25 parts by mass of tungsten trioxide with respect to 100 parts by mass of the carrier. preferable.
- the amount of the exhaust gas purifying catalyst supported on the bag filter is preferably 1 to 500 g / m 2 . Further, the loading amount of the exhaust gas purifying catalyst on the bag filter is more preferably 50 to 450 g / m 2 . If the amount of the exhaust gas purifying catalyst supported is not less than the lower limit (1 g / m 2 ), a sufficiently high exhaust gas purifying ability can be obtained, and if it is not more than the upper limit (500 g / m 2 ), Clogging can be prevented.
- the exhaust gas treatment system 1 of this example includes an exhaust gas treatment device 1a and a denitration device B that denitrates the exhaust gas treated by the exhaust gas treatment device 1a, and does not include a reheater.
- the exhaust gas denitrated by the denitration apparatus B is released from the chimney C into the atmosphere.
- This exhaust gas treatment method includes a temperature adjustment process, a reaction process, a removal process, and a denitration process.
- This exhaust gas treatment method treats exhaust gas discharged from the exhaust gas generator A of the exhaust gas treatment system 1 shown in FIG.
- the temperature adjustment process is a process in which the temperature of the exhaust gas discharged from the exhaust gas generator A is adjusted to an appropriate temperature at 190 ° C. or higher by the temperature control unit 10.
- the exhaust gas temperature is preferably adjusted to be more than 200 ° C. and less than 240 ° C.
- the exhaust gas temperature is more preferably adjusted to 220 ° C. or higher and lower than 240 ° C.
- the exhaust gas temperature is more preferably adjusted to 220 ° C. or more and 235 ° C. or less.
- the reaction process is a process of adding slaked lime to the exhaust gas whose temperature has been adjusted by the temperature adjustment process in the reaction unit 20 and causing the slaked lime and acid gas to react.
- the temperature of the exhaust gas is adjusted to 190 ° C. or higher, after slaked lime is added into the pipe 22 through which the exhaust gas passes by the slaked lime addition means 21, The reaction proceeds.
- activated carbon may be added to the exhaust gas together with slaked lime for the purpose of removing mercury in the exhaust gas.
- a removal process is a process of removing the reaction product obtained by the reaction process from waste gas using a bag filter.
- a reaction product when a sulfur oxide is included as an acidic gas, CaSO 4 can be mentioned.
- hydrogen chloride included as the acid gas
- CaCl 2 and the like can be mentioned.
- the removal step the reaction product contained in the exhaust gas is captured by the bag filter of the removal unit 30 and the exhaust gas is filtered. Thereby, acid gas content in exhaust gas is reduced. The reaction product captured by the bag filter is periodically removed from the bag filter and collected.
- the exhaust gas after the removal process is sent to the denitration apparatus B and denitrated.
- the exhaust gas denitrated by the denitration apparatus B is released from the chimney C into the atmosphere.
- NOx contained in the exhaust gas is decomposed and removed using a denitration apparatus B including a reactor filled with a denitration catalyst.
- a reducing agent such as ammonia may be used as necessary.
- the exhaust gas treatment system 2 of this example includes an exhaust gas treatment device 1a, and does not include a denitration device and a reheater.
- the exhaust gas discharged from the exhaust gas treatment device 1a is released from the chimney C into the atmosphere.
- This exhaust gas treatment method includes a temperature adjustment process, a reaction process, and a removal process.
- the exhaust gas is sent to the chimney C without passing through the denitration device, and the exhaust gas after the removal process is sent from the chimney C to the atmosphere. Release into.
- the temperature adjustment process, the reaction process, and the removal process in this example are the same as in the first example.
- the method of this example is applied when the nitrogen oxide content in the exhaust gas is low, or when the bag filter carrying the exhaust gas purifying catalyst having nitrogen oxide decomposability is used.
- the exhaust gas treatment system 5 of this example is the same as the conventional exhaust gas treatment system except that slaked lime having a specific surface area of 25 m 2 / g or more and a pore volume of 0.15 cm 3 / g or more is used. That is, the exhaust gas treatment system 5 of this example includes an exhaust gas treatment device 1a, a reheater D that reheats the exhaust gas that has passed through the exhaust gas treatment device 1a, and a denitration device B that denitrates the reheated exhaust gas. .
- the exhaust gas denitrated by the denitration apparatus B is released from the chimney C into the atmosphere.
- This exhaust gas treatment method includes a temperature adjustment process, a reaction process, a removal process, a reheating process, and a denitration process.
- This exhaust gas treatment method treats exhaust gas discharged from the exhaust gas generator A of the exhaust gas treatment system 5 shown in FIG. 11, then reheats the exhaust gas, and denitrates the reheated exhaust gas using the denitration device B. .
- the temperature adjustment process, reaction process, removal process, and denitration process in this example are the same as in the first example.
- the slaked lime used in the exhaust gas treatment apparatus 1a and the exhaust gas treatment method has a large specific surface area and pore volume, the reactivity with acidic gas is high. Therefore, sufficiently high acid gas removability can be ensured even in a temperature range where the reactivity of conventionally used slaked lime is low. Therefore, even if the temperature for reacting with the acid gas is 190 ° C. or higher, sufficient acid gas removability can be obtained without increasing the amount of slaked lime used.
- slaked lime and acidic gas are reacted at a high temperature as described above, a liquid material of highly corrosive acidic gas is hardly generated, and corrosion of the exhaust gas treatment apparatus 1a can be prevented.
- the amount of energy for reheating in the reheater D is slaked lime having a specific surface area of less than 25 m 2 / g and a pore volume of less than 0.15 cm 3 / g. This can be reduced as compared with the conventional method using. Further, depending on the denitration processing conditions, reheating can be omitted as in the first example and the second example.
- hydrogen chloride when hydrogen chloride is contained in the acidic gas, the reaction between the slaked lime and the sulfur oxide easily proceeds in the reaction between the slaked lime and the acidic gas. As a result, since desulfurization performance becomes higher, it is preferable that hydrogen chloride coexists in the acid gas.
- the slaked lime used in this embodiment has high reactivity, even if hydrogen chloride does not coexist, it has high reactivity with sulfur oxides, and high desulfurization performance can be obtained. Therefore, it is suitable for desulfurization of exhaust gas from an industrial waste incinerator having a low hydrogen chloride concentration in exhaust gas and exhaust gas from a sewage sludge incinerator.
- the exhaust gas treatment system of this embodiment includes an exhaust gas treatment device 2a shown in FIG.
- Exhaust gas treatment apparatus 2a of the present embodiment is the same as exhaust gas treatment apparatus 1a of the first embodiment except that it does not have a temperature control unit.
- the exhaust gas treatment apparatus 2a of this embodiment includes a reaction unit 20 and a removal unit 30. Therefore, also in the present embodiment, the slaked lime is reacted with the acidic gas in the exhaust gas, and the reaction product is captured by the bag filter.
- the second embodiment is applied when the temperature of the exhaust gas does not need to be adjusted by the temperature control unit, that is, when the temperature of the exhaust gas discharged from the exhaust gas generator is 190 ° C. or higher.
- the exhaust gas treatment system 3 of this example includes an exhaust gas treatment device 2a and a denitration device B that denitrates the exhaust gas treated by the exhaust gas treatment device 2a, and does not include a reheater.
- the exhaust gas denitrated by the denitration apparatus B is released from the chimney C into the atmosphere.
- This exhaust gas treatment method includes a reaction step, a removal step, and a denitration step.
- This exhaust gas treatment method treats exhaust gas discharged from the exhaust gas generator A of the exhaust gas treatment system 3 shown in FIG. That is, slaked lime is added to the exhaust gas exhausted from the exhaust gas generator A at the reaction unit 20 without adjusting the temperature at the temperature control unit to react the slaked lime with the acid gas.
- the removal step the reaction product formed in the reaction step is removed from the exhaust gas using the bag filter of the removal unit 30 to reduce the acid gas content in the exhaust gas. Then, the exhaust gas with reduced acid gas content is denitrated using the denitration device B, and the denitrated exhaust gas is discharged from the chimney C into the atmosphere.
- the exhaust gas treatment system 4 of this example includes an exhaust gas treatment device 2a, and does not include a denitration device and a reheater.
- the exhaust gas discharged from the exhaust gas treatment device 2a is released from the chimney C into the atmosphere.
- This exhaust gas treatment method has a reaction step and a removal step.
- the exhaust gas is sent to the chimney C without passing through the denitration device, and the exhaust gas after the removal process is sent from the chimney C to the atmosphere. Release into.
- the reaction step and the removal step in this example are the same as in the first example.
- the method of this example is applied when the nitrogen oxide content in the exhaust gas is low, or when the bag filter carrying the exhaust gas purifying catalyst having nitrogen oxide decomposability is used.
- the simulated exhaust gas containing 400 ppm of HCl and 50 ppm of SO 2 was subjected to acid gas removal treatment using a plurality of slaked lime having different BET specific surface areas and pore volumes. Specifically, slaked lime is added to the simulated exhaust gas, HCl and SO 2 are reacted with slaked lime at 220 ° C., and the obtained reaction product is captured by a bag filter (injection density: 900 g / m 2 ). Removed from the exhaust gas. The HCl and SO 2 concentrations in the exhaust gas after the acid gas removal treatment were measured, and the desalting rate (deHCl rate) and the desulfurization rate (deSO 2 rate) were determined.
- FIG. 7 shows a graph in which the horizontal axis is the BET specific surface area and the vertical axis is the desulfurization rate.
- FIG. 8 shows a graph in which the horizontal axis is the pore volume and the vertical axis is the desulfurization rate.
- FIG. 7 shows that the desulfurization rate is improved when the BET specific surface area of slaked lime is 25 m 2 / g or more.
- FIG. 8 shows that the desulfurization rate is improved when the pore volume of slaked lime is 0.15 cm 3 / g or more.
- slaked lime having a BET specific surface area of 40 m 2 / g and a pore volume of 0.3 cm 3 / g was added to a simulated exhaust gas containing 400 ppm of HCl and 50 ppm of SO 2. Slaked lime) was added to react HCl and SO 2 with slaked lime.
- slaked lime having a BET specific surface area of 15 m 2 / g and a pore volume of 0.07 cm 3 / g (a slaked lime conventionally used) containing simulated exhaust gas containing 400 ppm HCl and 50 ppm SO 2 was added to react HCl and SO 2 with slaked lime.
- the reaction product obtained by these reactions was captured by a bag filter (injection density: 900 g / m 2 ) and removed from the exhaust gas.
- the reaction temperature condition during the acid gas removal treatment is changed every 10 ° C.
- FIG. 9 shows a graph in which the horizontal axis is the reaction temperature and the vertical axis is the desalination rate.
- FIG. 10 shows a graph when the horizontal axis is the reaction temperature and the vertical axis is the desulfurization rate. From FIG. 9, in the slaked lime used conventionally, when the reaction temperature increases, the desalination rate decreases, whereas in the slaked lime used in the examples of the present invention, the desalination rate is increased even when the reaction temperature is increased.
- the slaked lime used in the past has a lower desulfurization rate when the reaction temperature is higher, whereas the slaked lime used in the examples of the present invention has a minimum desulfurization rate at around 185 ° C. It can be seen that the desulfurization rate becomes higher at 190 ° C. or higher.
- the specific surface area measured by the BET method is 25 m 2 / g or more, and the pore volume measured by the nitrogen desorption BJH method is 0.15 cm 3 /
- the specific surface area measured by the BET method is 25 m 2 / g or more
- the pore volume measured by the nitrogen desorption BJH method is 0.15 cm 3 /
Abstract
Description
図11に、酸性ガスを含む排ガスを処理する排ガス処理システムの一例を示す。前記排ガス処理システム5は、排ガス発生装置Aから排出した排ガスの温度を調整する温調部10と、前記排ガスに消石灰(ガス浄化剤)を添加する消石灰添加手段(ガス浄化剤添加手段)21を備える反応部20と、前記反応部20により得た反応生成物を排ガスから除去する除去部30と、反応生成物を除去した排ガスを再加熱する再加熱器Dと、再加熱した排ガスを脱硝処理する脱硝装置Bとを有する。
排ガス中の酸性ガスを除去する方法としては、消石灰添加手段21によって、排ガスに消石灰を添加し、消石灰と酸性ガスとを反応させた後、配管22を介して除去部30に供給し、得られた反応生成物を除去部30におけるバグフィルタ等を用いて除去する方法が広く採用されている。
従来使用していた消石灰においては、酸性ガスと反応させる温度を低くする程、反応性が高くなり、酸性ガスの除去率が高くなる傾向にあった(特許文献1,2)。そのため、従来の排ガス処理方法では、190℃未満で消石灰と酸性ガスとを反応させていた。
また、排ガス温度は220℃以上の高温であるため、酸性ガスと反応させる温度を190℃未満にするためには、排ガス温度を下げる処理が必要になる。そのため、図11に示すように、排ガスの温度を調整する温調部10を設けていた。さらに、酸性ガスを除去した排ガスに脱硝装置Bにて脱硝処理を施す場合には、脱硝反応に適した温度(210℃以上)にするために、再加熱器Dを用いて再加熱する必要があった。そのため、一旦温度を下げた後に再び上げることになり、エネルギーの消費量が多くなる傾向にあった。
一方、従来の消石灰を用いた場合、酸性ガスと反応させる温度を高くすると、反応性が不充分になるため、消石灰の使用量が多くなる傾向にあった。
本発明は、酸性ガスと反応させる温度を高く(具体的には190℃以上に)しても、消石灰の使用量を増やすことなく、充分な酸性ガス除去性が得られる排ガス処理方法、排ガス処理装置、及び、排ガス処理システムを提供する。
上記排ガス処理方法においては、前記バグフィルタに、排ガス浄化用触媒が担持されてもよい。
上記排ガス処理方法における反応工程では、消石灰と共に活性炭を添加してもよい。
上記排ガス処理装置においては、前記バグフィルタに、排ガス浄化用触媒が担持されていてもよい。
上記排ガス処理装置においては、前記ガス浄化剤は、活性炭をさらに含んでもよい。
上記排ガス処理システムにおいては、反応部の前段で、排ガス温度を190℃以上に調整する温調部を備えてもよい。
上記排ガス処理システムにおいては、除去部の後段に、排ガスを脱硝処理する脱硝装置を備えてもよい。
上記排ガス処理システムにおいては、除去部と脱硝装置の間に、排ガスを再加熱する再加熱器を備えてもよい。
上記排ガス処理システムにおいては、バグフィルタに、排ガス浄化用触媒が担持されていてもよい。
上記排ガス処理システムにおいては、前記ガス浄化剤は、活性炭をさらに含んでもよい。
上述した排ガス処理方法、排ガス処理装置、及び、排ガス処理システムにおいては、バグフィルタとして、排ガス浄化用触媒が担持されたものを用いると、排ガス中に含まれるダイオキシンや窒素酸化物を除去することも可能になるため、排ガスをより浄化させることができる。
また、排ガス処理方法、排ガス処理装置、及び、排ガス処理システムにおいて、消石灰と共に活性炭を添加すると、排ガス中の水銀を除去することができる。
本発明の排ガス処理システムの第1実施形態について説明する。
本実施形態の排ガス処理システムは、図1に示す排ガス処理装置1aを具備する。本実施形態の排ガス処理装置1aは、温調部10と、反応部20と、除去部30と、を有し、酸性ガスを含む排ガスを処理して、酸性ガスを排ガスから除去する装置である。
上記排ガスに含まれる酸性ガスとしては、塩化水素、硫黄酸化物、フッ化水素、等が挙げられる。
通常、排ガスは高温で排出されるため、温調部10としては、排ガス温度を下げる冷却装置等が使用される。冷却装置としては、熱交換器を利用したもの等が挙げられる。
本実施形態における排ガス処理装置1aでは、温調部10と除去部30とを接続する配管22に、消石灰添加手段21が接続されている。具体的には、反応部20は、配管22における、消石灰添加手段21によって消石灰が添加された部分から除去部30までの間の部分である。ただし、除去部30においても、消石灰と酸性ガスとの反応は生じる。
消石灰添加手段21としては、既存の装置や手段を使用することができる。
また、反応部20では、排ガス中の水銀を除去する目的で、消石灰と共に活性炭を排ガスに添加してもよい。
一方、入手容易性の観点からは、消石灰のBET比表面積は、60m2/g以下であることが好ましい。細孔容積は、0.3cm3/g以下であることが好ましい。
BET比表面積は、消石灰を脱ガスした後に、77Kで窒素を吸着させることにより測定して得た値である。細孔容積は、消石灰を脱ガスした後に、77Kで窒素を吸着させ、さらに窒素を脱着することにより測定して得た値である。BET比表面積及び細孔容積は、市販の測定装置により測定することができる。測定装置としては、例えば、マイクロメリティックス社製比表面積・細孔分布測定装置ASAPシリーズ等が挙げられる。
消石灰の平均粒子径は、5~12μmであることが好ましい。また、消石灰の平均粒子径は、7~10μmであることがより好ましい。ここで、平均粒子径は、レーザー粒度測定装置やSEM観察によって測定される値である。
除去部30では、反応生成物を含む排ガスをバグフィルタに供給し、反応生成物をバグフィルタにより捕捉する。これにより、バグフィルタを通過した排ガスの酸性ガス含有量が少なくなる。
バグフィルタに捕捉された反応生成物は、定期的に払い落とされ、除去部30から取り除かれる。
バグフィルタを構成する繊維としては、例えば、ガラス繊維、ポリフルオロエチレン系繊維、ポリエステル系繊維、ポリアミド系繊維、ポリフェニレンサルファイド系繊維等が挙げられる。前記繊維のうちでも、耐熱性が高い点では、ガラス繊維及びポリフルオロエチレン系繊維が好ましい。繊維の直径は、3~15μmが好ましい。
バグフィルタに担持する排ガス浄化用触媒が窒素酸化物分解性を有するものであれば、排ガス中の窒素酸化物含有量が低くなり、バグフィルタ以外の脱硝処理を省略することができる。
バグフィルタに担持する排ガス浄化用触媒がダイオキシン分解性を有するものであれば、排ガス中のダイオキシン含有量が低くなる。一般に、温度を高くする程、ダイオキシン除去性が低くなる傾向にある。しかしながら、ダイオキシン分解性を有する排ガス浄化用触媒がバグフィルタに担持されていれば、190℃以上の温度にしても、190℃未満の温度の場合と同様のダイオキシン除去性が得られる。
担体としては、少なくともチタン酸化物を用いることが好ましい。
活性成分としては、少なくともバナジウム酸化物を用いることが好ましい。上記活性成分は、いずれも酸化能力を有し、ダイオキシンを酸化分解できる。また、上記活性成分はいずれも、還元剤存在下で窒素酸化物を還元できる。上記活性成分の中で、バナジウム酸化物は、それらの能力が特に優れる。
活性成分が五酸化バナジウムと三酸化タングステンの二成分である場合には、担体100質量部に対して、五酸化バナジウムが1~10質量部、三酸化タングステンが2~25質量部であることが好ましい。
本例の排ガス処理システム1は、排ガス処理装置1aと、排ガス処理装置1aで処理された排ガスを脱硝処理する脱硝装置Bとを備え、再加熱器を備えない。脱硝装置Bによって脱硝された排ガスは、煙突Cから大気中に放出される。
この排ガス処理方法は、温調工程と、反応工程と、除去工程と、脱硝工程と、を有する。この排ガス処理方法は、図2に示す排ガス処理システム1の排ガス発生装置Aから排出された排ガスを処理し、脱硝装置Bにて脱硝処理する。
反応工程では、排ガス中の水銀を除去する目的で、消石灰と共に活性炭を排ガスに添加してもよい。
具体的に除去工程では、排ガスに含まれる反応生成物を、除去部30のバグフィルタにより捕捉して排ガスをろ過する。これにより、排ガス中の酸性ガス含有量を低減させる。
バグフィルタにより捕捉された反応生成物は、定期的にバグフィルタから払い落とされて集塵される。
本例の排ガス処理システム2は、排ガス処理装置1aを備え、脱硝装置及び再加熱器を備えない。排ガス処理装置1aから排出された排ガスは、煙突Cから大気中に放出される。
この排ガス処理方法は、温調工程と、反応工程と、除去工程とを有する。この排ガス処理方法は、図3に示す排ガス処理システム2の排ガス発生装置Aから排出された排ガスを処理した後、脱硝装置を通さずに煙突Cに送り出し、除去工程後の排ガスを煙突Cから大気中に放出する。本例における温調工程と、反応工程と、除去工程とは、上記第1の例と同様である。
排ガス中の窒素酸化物含有量が少ない場合、あるいは、窒素酸化物分解性を有する排ガス浄化用触媒が担持されたバグフィルタを用いる場合に、本例の方法は適用される。
本例の排ガス処理システム5は、比表面積が25m2/g以上、且つ、細孔容積が0.15cm3/g以上の消石灰を用いた点以外は、従来の排ガス処理システムと同様である。すなわち、本例の排ガス処理システム5は、排ガス処理装置1aと、排ガス処理装置1aを経た排ガスを再加熱する再加熱器Dと、再加熱された排ガスを脱硝処理する脱硝装置Bと、を備える。脱硝装置Bによって脱硝された排ガスは、煙突Cから大気中に放出される。
この排ガス処理方法は、温調工程と、反応工程と、除去工程と、再加熱工程と、脱硝工程と、を有する。この排ガス処理方法は、図11に示す排ガス処理システム5の排ガス発生装置Aから排出された排ガスを処理した後、排ガスを再加熱し、再加熱した排ガスを、脱硝装置Bを用いて脱硝処理する。本例における温調工程と、反応工程と、除去工程と、脱硝工程とは、上記第1の例と同様である。
本実施形態では、上記のように、消石灰と酸性ガスとを高い温度で反応させるため、腐食性が高い酸性ガスの液状物が生じにくく、排ガス処理装置1aの腐食を防止できる。また、除去工程後の排ガスに脱硝処理を施す場合、再加熱器Dにおける再加熱のためのエネルギー量を、比表面積が25m2/g未満且つ細孔容積が0.15cm3/g未満の消石灰を用いた従来法よりも削減できる。さらに、脱硝処理条件によっては、上記第1の例及び上記第2の例のように再加熱を省略することができる。
一般に、酸性ガスに塩化水素が含まれる場合、消石灰と酸性ガスとの反応においては、消石灰と硫黄酸化物との反応が進みやすくなる。この結果、脱硫性能がより高くなることから、酸性ガス中に塩化水素が共存していることが好ましい。しかし、本実施形態で使用する消石灰は反応性が高いため、塩化水素が共存しなくても、硫黄酸化物との反応性が高く、高い脱硫性能を得ることができる。そのため、排ガス中の塩化水素濃度が低い産業廃棄物焼却炉からの排ガス及び下水汚泥焼却炉からの排ガスの脱硫に好適である。
本発明の排ガス処理システムの第2実施形態について説明する。
本実施形態の排ガス処理システムは、図4に示す排ガス処理装置2aを具備する。本実施形態の排ガス処理装置2aは、温調部を有さない以外は第1実施形態の排ガス処理装置1aと同様である。本実施形態の排ガス処理装置2aは、反応部20と除去部30とを有する。したがって、本実施形態でも、上記の消石灰を排ガス中の酸性ガスに反応させ、バグフィルタによって反応生成物を捕捉する。
第2実施形態は、排ガスの温度を温調部によって調整しなくてもよい場合、すなわち、排ガス発生装置から排出された排ガスの温度が190℃以上になっている場合に適用される。
本例の排ガス処理システム3は、排ガス処理装置2aと、排ガス処理装置2aで処理された排ガスを脱硝処理する脱硝装置Bとを備え、再加熱器を備えない。脱硝装置Bによって脱硝された排ガスは、煙突Cから大気中に放出される。
この排ガス処理方法は、反応工程と、除去工程と、脱硝工程と、を有する。この排ガス処理方法は、図5に示す排ガス処理システム3の排ガス発生装置Aから排出された排ガスを処理し、脱硝装置Bにて脱硝処理する。
すなわち、排ガス発生装置Aから排出された排ガスに、温調部にて温度を調整することなく、反応部20にて、消石灰を添加して、消石灰と酸性ガスとを反応させる。次いで、除去工程において、反応工程にて形成した反応生成物を、除去部30のバグフィルタを用いて排ガスから除去して、排ガス中の酸性ガス含有量を低減させる。そして、酸性ガス含有量を低減させた排ガスを、脱硝装置Bを用いて脱硝処理し、脱硝処理した排ガスを煙突Cから大気中に放出する。
本例の排ガス処理システム4は、排ガス処理装置2aを備え、脱硝装置及び再加熱器を備えない。排ガス処理装置2aから排出された排ガスは、煙突Cから大気中に放出される。
この排ガス処理方法は、反応工程と除去工程とを有する。この排ガス処理方法は、図6に示す排ガス処理システム4の排ガス発生装置Aから排出された排ガスを処理した後、脱硝装置を通さずに煙突Cに送り出し、除去工程後の排ガスを煙突Cから大気中に放出する。本例における反応工程と除去工程は、上記第1の例と同様である。
排ガス中の窒素酸化物含有量が少ない場合、あるいは、窒素酸化物分解性を有する排ガス浄化用触媒が担持されたバグフィルタを用いる場合に、本例の方法は適用される。
それに加えて、本実施形態では、排ガスの温度を調整することなく、排ガス中の酸性ガスと消石灰とを反応させるため、酸性ガスを除去する装置の構成を簡略化できる。
酸性ガス除去処理後の排ガス中のHCl及びSO2濃度を測定し、脱塩率(脱HCl率)及び脱硫率(脱SO2率)を求めた。
図7に、横軸をBET比表面積とし、縦軸を脱硫率とした場合のグラフを示す。図8に、横軸を細孔容積とし、縦軸を脱硫率とした場合のグラフを示す。
図7より、消石灰のBET比表面積が25m2/g以上になると、脱硫率が向上することが分かる。図8より、消石灰の細孔容積が0.15cm3/g以上になると、脱硫率が向上することが分かる。
上記酸性ガス除去処理の際の反応温度条件を150~220℃の間で10℃ごとに変え、酸性ガス除去処理後の排ガス中のHCl及びSO2濃度を各々測定し、脱塩率(脱HCl率)及び脱硫率(脱SO2率)を求めた。
図9に、横軸を反応温度とし、縦軸を脱塩率とした場合のグラフを示す。図10に、横軸を反応温度とし、縦軸を脱硫率とした場合のグラフを示す。
図9より、従来使用されていた消石灰では、反応温度が高くなると、脱塩率が低下するのに対し、本発明の実施例で使用する消石灰では、反応温度が高くなっても、脱塩率を維持できることが分かる。
図10より、従来使用されていた消石灰では、反応温度が高くなると、脱硫率が低下するのに対し、本発明の実施例で使用する消石灰では、反応温度が185℃付近で脱硫率が極小となり、190℃以上になると、かえって脱硫率が高くなることが分かる。
1a,2a 排ガス処理装置
10 温調部
20 反応部
21 消石灰添加手段(ガス浄化剤添加手段)
30 除去部
A 排ガス発生装置
B 脱硝装置
C 煙突
D 再加熱器
Claims (12)
- 酸性ガスを含む排ガスに消石灰を添加し、消石灰と酸性ガスを190℃以上で反応させる反応工程と、
前記反応工程により得た反応生成物を、バグフィルタを用いて排ガスから除去する除去工程と、を備え、
前記消石灰は、BET法により測定した比表面積が25m2/g以上、且つ、窒素脱着BJH法により測定した細孔容積が0.15cm3/g以上である、
排ガス処理方法。 - 請求項1に記載の排ガス処理方法であって、
前記バグフィルタに、排ガス浄化用触媒が担持されている排ガス処理方法。 - 請求項1または2に記載の排ガス処理方法であって、
前記反応工程では、消石灰と共に活性炭を添加する、排ガス処理方法。 - 酸性ガスを含む190℃以上の排ガスにガス浄化剤を添加するガス浄化剤添加手段を備え、ガス浄化剤と酸性ガスを反応させる反応部と、
前記反応部により得た反応生成物を排ガスから除去するバグフィルタを備える除去部と、を備え、
前記ガス浄化剤が、BET法により測定した比表面積が25m2/g以上、且つ、窒素脱着BJH法により測定した細孔容積が0.15cm3/g以上の消石灰を含む
排ガス処理装置。 - 請求項4に記載の排ガス処理装置であって、
前記バグフィルタに、排ガス浄化用触媒が担持されている、排ガス処理装置。 - 請求項4または5に記載の排ガス処理装置であって、
前記ガス浄化剤は、活性炭をさらに含む、排ガス処理装置。 - 酸性ガスを含む190℃以上の排ガスにガス浄化剤を添加するガス浄化剤添加手段を備え、ガス浄化剤と酸性ガスを反応させる反応部と、
前記反応部により得た反応生成物を排ガスから除去するバグフィルタを備える除去部と、を備え、
前記ガス浄化剤が、BET法により測定した比表面積が25m2/g以上、且つ、窒素脱着BJH法により測定した細孔容積が0.15cm3/g以上の消石灰を含む
排ガス処理システム。 - 請求項7に記載の排ガス処理システムであって、
反応部の前段で、排ガス温度を190度以上に調整する温調部をさらに備える、排ガス処理システム。 - 請求項7または8に記載の排ガス処理システムであって、
除去部の後段に、排ガスを脱硝処理する脱硝装置をさらに備える、排ガス処理システム。 - 請求項9に記載の排ガス処理システムであって、
除去部と脱硝装置の間に、排ガスを再加熱する再加熱器をさらに備える排ガス処理システム。 - 請求項7~10のいずれか1項に記載の排ガス処理システムであって、
バグフィルタに排ガス浄化用触媒が担持されている、排ガス処理システム。 - 請求項7~11のいずれか1項に記載の排ガス処理システムであって、
前記ガス浄化剤は、活性炭をさらに含む、排ガス処理システム。
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JP2000107562A (ja) * | 1998-10-06 | 2000-04-18 | Babcock Hitachi Kk | 燃焼排ガスの処理装置 |
JP2000317264A (ja) * | 1999-05-17 | 2000-11-21 | Nkk Corp | 排ガス中の有害成分除去方法および排ガス処理装置 |
JP2004237249A (ja) * | 2003-02-07 | 2004-08-26 | Okutama Kogyo Co Ltd | 排ガス処理方法 |
JP2012245444A (ja) * | 2011-05-25 | 2012-12-13 | Nippon Steel Corp | 焼結炉排ガスの脱硫・脱硝方法 |
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SG11201506300WA (en) | 2015-09-29 |
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JP2014184423A (ja) | 2014-10-02 |
AU2014220033A1 (en) | 2015-08-27 |
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CN104994935A (zh) | 2015-10-21 |
US20150375168A1 (en) | 2015-12-31 |
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