KR20240046446A - Nitrogen oxide reduction device comprising catalyst for decomposition of nitric oxide - Google Patents
Nitrogen oxide reduction device comprising catalyst for decomposition of nitric oxide Download PDFInfo
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 155
- 239000003054 catalyst Substances 0.000 title claims abstract description 78
- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000007789 gas Substances 0.000 claims abstract description 44
- 238000002485 combustion reaction Methods 0.000 claims abstract description 26
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000001301 oxygen Substances 0.000 claims abstract description 13
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 13
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- 229910044991 metal oxide Inorganic materials 0.000 claims description 5
- 150000004706 metal oxides Chemical class 0.000 claims description 5
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 229910052697 platinum Inorganic materials 0.000 claims description 3
- 229910052703 rhodium Inorganic materials 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 21
- 238000000034 method Methods 0.000 abstract description 10
- 239000003638 chemical reducing agent Substances 0.000 abstract description 9
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 abstract description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 abstract description 3
- 238000007796 conventional method Methods 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 17
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 229910010413 TiO 2 Inorganic materials 0.000 description 3
- 239000000809 air pollutant Substances 0.000 description 3
- 231100001243 air pollutant Toxicity 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- MGWGWNFMUOTEHG-UHFFFAOYSA-N 4-(3,5-dimethylphenyl)-1,3-thiazol-2-amine Chemical compound CC1=CC(C)=CC(C=2N=C(N)SC=2)=C1 MGWGWNFMUOTEHG-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical group [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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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
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8628—Processes characterised by a specific catalyst
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
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- B01D2255/102—Platinum group metals
- B01D2255/1021—Platinum
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1025—Rhodium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/206—Rare earth metals
- B01D2255/2066—Praseodymium
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- 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
- B01D2255/20761—Copper
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- 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
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Abstract
본 발명은 일산화질소(NO)를 포함하는 배가스를 배출하는 연소로 및 상기 연소로 후단에 구비된 일산화질소(NO) 분해 촉매를 포함하고, 상기 촉매는 상기 배가스와 접촉하여 일산화질소(NO)를 질소(N2) 및 산소(O2)로 직접 분해하는 질소산화물 저감 장치를 제공한다. 본 발명에 의하면, 장치 구성이 비교적 단순하고 공정 비용 또한 경제적이고, 환원제 시약을 사용할 필요가 없으므로 종래 암모니아수와 같은 환원제를 사용하는 방법에 비해 비용이 저렴하고, 추가적인 승온 공정이 필요하지 않으므로 에너지를 절감할 수 있는 이점이 있다. 또한, 본 발명은 연소로 후단에 질소산화물 분해 촉매를 구비하여 일산화질소(NO)를 질소 및 산소로 직접 분해함으로써 배가스로부터 질소산화물(NOx)을 제거할 수 있다.The present invention includes a combustion furnace that discharges exhaust gas containing nitrogen monoxide (NO) and a nitrogen monoxide (NO) decomposition catalyst provided at a rear end of the combustion furnace, wherein the catalyst contacts the exhaust gas to produce nitrogen monoxide (NO). A nitrogen oxide reduction device that directly decomposes into nitrogen (N 2 ) and oxygen (O 2 ) is provided. According to the present invention, the device configuration is relatively simple, the process cost is also economical, and there is no need to use a reducing agent, so the cost is lower than the conventional method using a reducing agent such as ammonia water, and energy is saved because an additional temperature raising process is not required. There are benefits to doing this. In addition, the present invention can remove nitrogen oxides (NOx) from exhaust gas by directly decomposing nitrogen monoxide (NO) into nitrogen and oxygen by providing a nitrogen oxide decomposition catalyst at the rear end of the combustion furnace.
Description
본 발명은 일산화질소(NO) 분해 촉매를 포함하는 질소산화물 저감 장치에 관한 것으로, 보다 상세하게는 고온의 배가스가 배출되는 연소로 후단에 일산화질소 분해 촉매를 구비함으로써 환원제를 사용하지 않고도 질소산화물이 대기중으로 배출되는 것을 저감시킬 수 있는 질소산화물 저감 장치에 관한 것이다.The present invention relates to a nitrogen oxide reduction device including a nitrogen monoxide (NO) decomposition catalyst, and more specifically, by providing a nitrogen monoxide decomposition catalyst at the rear of the combustion furnace where high temperature exhaust gas is discharged, nitrogen oxides are reduced without using a reducing agent. This relates to a nitrogen oxide reduction device that can reduce emissions into the atmosphere.
발전소, 제철소 등 에너지를 사용하는 산업체는 석탄, 가스 등의 연료를 이용한 다양한 연소 시설을 운영한다. 이 때 발생하는 산소와 질소 반응에 의해 질소산화물(NOx)과 같은 대기 오염 물질이 필수적으로 발생한다. 따라서, 대기 오염 물질을 발생시키는 모든 사업장은 유해가스의 배출을 저감시키기 위해 많은 비용과 노력을 들이고 있다.Industries that use energy, such as power plants and steel mills, operate various combustion facilities using fuels such as coal and gas. At this time, air pollutants such as nitrogen oxides (NOx) are inevitably generated due to the reaction between oxygen and nitrogen. Therefore, all businesses that generate air pollutants are investing a lot of money and effort to reduce emissions of harmful gases.
정부의 미세먼지 정책 강화로 인해 배출허용농도가 점차 낮아지고 있으며, 배출 총량에 대해서도 관리가 필요하므로 이러한 산성물질을 제거하기 위한 다양한 연구가 행해지고 있으며, 주로, 연소제어를 통해 이산화질소(NO2)가 발생하지 않게 하거나, 후처리 기술로, SCR(Selective Catalyst Reduction, 선택적 촉매 환원), SNCR(Selective Noncatalytic Reduction, 선택적 비촉매 환원) 또는 산성가스를 흡입한 후 중화된 가스를 배출시키는 스크러버(Scrubber)를 통해 제거하는 방법 등이 제안되어 있다.Due to the strengthening of the government's fine dust policy, the allowable emission concentration is gradually lowering, and the total amount of emissions also needs to be managed, so various studies are being conducted to remove these acidic substances. Mainly, nitrogen dioxide (NO 2 ) is reduced through combustion control. To prevent it from occurring, or as a post-treatment technology, use SCR (Selective Catalyst Reduction), SNCR (Selective Noncatalytic Reduction), or a scrubber that inhales acid gas and discharges the neutralized gas. Methods for removing it are proposed.
그러나, SCR 또는 SNCR 방법의 경우, 산성물질을 제거하기 위해 환원제로 사용되는 약품비용이 과다하게 소모되어, 운영비가 증가하는 문제가 있고, 고온 하에 공정을 수행해야 하므로 가열 공정을 위한 비용이 발생하며, 공정 후단에서 미반응 환원제가 배출되지 않도록 관리해야 하는 문제가 있다.However, in the case of the SCR or SNCR method, the cost of chemicals used as reducing agents to remove acidic substances is excessively consumed, which increases operating costs, and the process must be performed at high temperatures, which incurs costs for the heating process. , there is a problem that must be managed to prevent unreacted reducing agent from being discharged at the rear end of the process.
이에, 환원제를 사용하지 않고 공간 및 비용을 최소화하며 배가스에 포함된 질소산화물을 저감할 수 있는 촉매 및 장치가 제공되는 경우 관련 분야에서 유용하게 사용될 수 있을 것으로 기대된다.Accordingly, if a catalyst and device are provided that can reduce nitrogen oxides contained in exhaust gas while minimizing space and cost without using a reducing agent, it is expected to be useful in related fields.
본 발명은 연료를 연소시키는 장치에 일산화질소(NO) 분해 촉매를 구비함으로써 구성이 비교적 단순하고 공정 비용 또한 경제적인 질소산화물(NOx) 저감 장치를 제공하고자 한다.The present invention seeks to provide a nitrogen oxide (NOx) reduction device that is relatively simple in construction and economical in process cost by providing a nitrogen monoxide (NO) decomposition catalyst in a fuel combustion device.
본 발명의 일 측면에 따르면, 일산화질소(NO)를 포함하는 배가스를 배출하는 연소로 및 상기 연소로 후단에 구비된 일산화질소(NO) 분해 촉매를 포함하고, 상기 촉매는 상기 배가스와 접촉하여 일산화질소(NO)를 질소(N2) 및 산소(O2)로 분해하는, 질소산화물 저감 장치가 제공된다.According to one aspect of the present invention, it includes a combustion furnace for discharging exhaust gas containing nitrogen monoxide (NO) and a nitrogen monoxide (NO) decomposition catalyst provided at a rear end of the combustion furnace, wherein the catalyst contacts the exhaust gas to oxidize the exhaust gas. A nitrogen oxide reduction device is provided that decomposes nitrogen (NO) into nitrogen (N 2 ) and oxygen (O 2 ).
본 발명에 의하면, 장치 구성이 비교적 단순하고 공정 비용 또한 경제적인 질소산화물(NOx) 저감 장치가 제공된다. According to the present invention, a nitrogen oxide (NOx) reduction device is provided that has a relatively simple device configuration and is economical in process cost.
본 발명은 환원제 시약을 사용할 필요가 없으므로 종래 암모니아수와 같은 환원제를 사용하는 방법에 비해 비용이 저렴하고, 추가적인 승온 공정이 필요하지 않으므로 에너지를 절감할 수 있는 이점이 있다.Since the present invention does not require the use of a reducing reagent, the cost is lower than that of a conventional method using a reducing agent such as ammonia water, and it has the advantage of saving energy because it does not require an additional temperature raising process.
본 발명은 연소로 후단에 질소산화물 분해 촉매를 구비하여 일산화질소(NO)를 질소 및 산소로 직접 분해함으로써 배가스로부터 질소산화물(NOx)을 제거할 수 있다.The present invention can remove nitrogen oxides (NOx) from exhaust gas by directly decomposing nitrogen monoxide (NO) into nitrogen and oxygen by providing a nitrogen oxide decomposition catalyst at the rear end of the combustion furnace.
도 1은 본 발명의 질소산화물 저감 장치의 간략한 모식도를 나타낸 것이다.
도 2는 종래 기술의 질소산화물 저감 장치의 간략한 모식도를 나타낸 것으로, 연소로(1) 및 암모니아수의 주입 노즐(2)을 포함하는 장치를 사용하여 질소산화물을 질소로 전환시킨 후 배출하는 것이다.
도 3은 Al2O3 지지체에 Cu를 함유하는 촉매(촉매 1)를 사용하여 800 내지 1000℃에서 일산화질소 전환율을 측정한 것이다.
도 4는 CeO2 지지체에 Rh를 함유하는 촉매(촉매 2)를 사용하여 600 내지 800℃에서 일산화질소 전환율을 측정한 것이다.
도 5는 PrO2 지지체에 Rh를 함유하는 촉매(촉매 4)를 사용하여 450 내지 800℃에서 일산화질소 전환율을 측정한 것이다.
도 6은 PrO2를 단독으로 사용한 촉매(촉매 3)의 XRD 결과를 나타낸 것이다.Figure 1 shows a brief schematic diagram of the nitrogen oxide reduction device of the present invention.
Figure 2 shows a simplified schematic diagram of a nitrogen oxide reduction device of the prior art, in which nitrogen oxides are converted to nitrogen and then discharged using a device including a combustion furnace (1) and an ammonia water injection nozzle (2).
Figure 3 shows the nitrogen monoxide conversion rate measured at 800 to 1000°C using a catalyst (catalyst 1) containing Cu on an Al 2 O 3 support.
Figure 4 shows the nitrogen monoxide conversion rate measured at 600 to 800°C using a catalyst (catalyst 2) containing Rh on a CeO 2 support.
Figure 5 shows the nitrogen monoxide conversion rate measured at 450 to 800°C using a catalyst (catalyst 4) containing Rh on a PrO 2 support.
Figure 6 shows the XRD results of a catalyst (catalyst 3) using PrO 2 alone.
이하, 본 발명의 바람직한 실시 형태를 설명한다. 그러나, 본 발명의 실시 형태는 여러 가지 다른 형태로 변형될 수 있으며, 본 발명의 범위가 이하 설명하는 실시 형태로 한정되는 것은 아니다.Hereinafter, preferred embodiments of the present invention will be described. However, the embodiments of the present invention may be modified into various other forms, and the scope of the present invention is not limited to the embodiments described below.
본 발명은 배가스와 접촉하여 상기 배가스에 포함된 일산화질소를 분해하는 촉매가 구비된 질소산화물 저감 장치에 관한 것이다.The present invention relates to a nitrogen oxide reduction device equipped with a catalyst that contacts exhaust gas and decomposes nitrogen monoxide contained in the exhaust gas.
구체적으로, 본 발명의 장치는 일산화질소(NO)를 포함하는 배가스를 배출하는 연소로 및 연소로 후단에 구비된 일산화질소(NO) 분해 촉매를 포함하고, 상기 촉매는 상기 배가스와 접촉하여 일산화질소(NO)를 질소(N2) 및 산소(O2)로 분해할 수 있다.Specifically, the device of the present invention includes a combustion furnace that discharges exhaust gas containing nitrogen monoxide (NO) and a nitrogen monoxide (NO) decomposition catalyst provided at the rear of the combustion furnace, and the catalyst contacts the exhaust gas to produce nitrogen monoxide. (NO) can be decomposed into nitrogen (N 2 ) and oxygen (O 2 ).
본 발명의 연소로는 보일러, 발전소, 소각로 등 배가스를 배출하는 각종 연소시설을 의미하고, 본 발명은 연료를 연소시키는 공정에서 발생되는 생활 배가스 및 산업 배가스 등의 배가스를 처리 대상으로 한다.The combustion furnace of the present invention refers to various combustion facilities that emit exhaust gases, such as boilers, power plants, and incinerators, and the present invention is intended to treat exhaust gases such as household exhaust gas and industrial exhaust gas generated in the process of burning fuel.
본 발명의 촉매는 일산화질소(NO)를 질소(N2) 및 산소(O2)로 직접 분해하는 것(식 1)으로, 암모니아(NH3)와 같은 환원제의 사용(식 2) 없이도 일산화질소를 직접 분해하여 질소를 생성할 수 있다.The catalyst of the present invention decomposes nitrogen monoxide (NO) directly into nitrogen (N 2 ) and oxygen (O 2 ) (Equation 1), thereby producing nitrogen monoxide without the use of a reducing agent such as ammonia (NH 3 ) (Equation 2). Nitrogen can be produced by direct decomposition.
식 1: 2NO → N2 + O2 Equation 1: 2NO → N 2 + O 2
식 2: 4NO + 4NH3 + O2 → 4N2 + 6H2OFormula 2: 4NO + 4NH 3 + O 2 → 4N 2 + 6H 2 O
상기 촉매는 일산화질소를 직접 분해할 수 있는 것이라면 제한 없이 사용할 수 있고 특별하게 한정되지 않으나, 금속산화물을 촉매 지지체로 하여 활성 금속이 담지된 촉매일 수 있다. The catalyst can be used without limitation as long as it can directly decompose nitrogen monoxide, and is not particularly limited, but may be a catalyst in which an active metal is supported using a metal oxide as a catalyst support.
상기 금속산화물은 PrO2, CeO2, ZrO2, TiO2 및 Al2O3 로 이루어진 그룹에서 선택되는 적어도 하나일 수 있다. 또한, 상기 활성 금속은 Cu, Pt, Rh, Ru 및 Pd로 이루어진 그룹에서 선택되는 적어도 하나일 수 있다. 예를 들어, 본 발명의 산화 촉매는 PrO2, CeO2, TiO2 및 Al2O3 지지체 상에 활성 금속으로서 Pt, Cu 또는 Rh 등의 금속이 담지된 촉매일 수 있다. 보다 바람직하게는 PrO2 지지체에 Rh를 담지한 것일 수 있다. The metal oxide may be at least one selected from the group consisting of PrO 2 , CeO 2 , ZrO 2 , TiO 2 and Al 2 O 3 . Additionally, the active metal may be at least one selected from the group consisting of Cu, Pt, Rh, Ru, and Pd. For example, the oxidation catalyst of the present invention may be a catalyst in which metals such as Pt, Cu or Rh are supported as active metals on PrO 2 , CeO 2 , TiO 2 and Al 2 O 3 supports. More preferably, Rh may be supported on a PrO 2 support.
또한, 상기 촉매는 상기 금속산화물 자체를 촉매로 사용할 수 있다. 바람직하게는, 예를 들어 PrO2를 촉매로 사용할 수 있다.Additionally, the catalyst may use the metal oxide itself as a catalyst. Preferably, for example, PrO 2 can be used as a catalyst.
본 발명의 촉매가 지지체에 활성 금속이 담지된 촉매인 경우 활성 금속의 함량은 촉매 전체 중량에 대하여 0 초과 내지 30 중량%일 수 있고, 바람직하게는 0 초과 내지 20 중량%일 수 있다. 함량이 30 중량% 초과인 경우, 촉매 효율에 비해 비용이 증가하므로 비경제적이다.When the catalyst of the present invention is a catalyst in which an active metal is supported on a support, the content of the active metal may be greater than 0 to 30% by weight, preferably greater than 0 to 20% by weight, based on the total weight of the catalyst. If the content exceeds 30% by weight, the cost increases compared to the catalyst efficiency, making it uneconomical.
상기 촉매는 촉매의 구성에 따라 활성을 갖는 온도 범위가 다양하므로 본 발명의 장치가 촉매를 다양하게 구비하는 경우 보다 넓은 온도 범위에서 배가스 내에 포함된 일산화질소를 직접 분해할 수 있다.Since the temperature range at which the catalyst is active varies depending on the composition of the catalyst, if the device of the present invention is equipped with a variety of catalysts, it can directly decompose nitrogen monoxide contained in the exhaust gas over a wider temperature range.
본 발명의 상기 일산화질소를 포함하는 배가스는 연소로에서 배출되는 것으로 온도가 500 내지 1000℃일 수 있고, 바람직하게는 550 내지 850℃일 수 있다.The exhaust gas containing nitrogen monoxide of the present invention is discharged from a combustion furnace and may have a temperature of 500 to 1000°C, preferably 550 to 850°C.
상기 배가스와 접촉하는 촉매는 500 내지 1000℃, 바람직하게는 550 내지 850℃인 배가스의 온도 범위 내에서 활성을 가질 수 있으며, 일산화탄소 직접 분해를 위해서는 배가스와 촉매가 접촉하는 동안 온도가 유지되는 것이 중요하므로 상기 촉매는 고온의 배가스와 직접적으로 접촉할 수 있는 연소로 내부에 구비될 수 있다. 구체적으로, 상기 온도 범위 내에서 촉매의 활성이 가장 우수하므로, 연소로 후단에 촉매가 구비되는 경우 고온의 배가스가 연소로에서 배출될 때 상기 촉매와 접촉할 수 있으므로 바람직하다.The catalyst in contact with the exhaust gas may be active within the temperature range of the exhaust gas, which is 500 to 1000°C, preferably 550 to 850°C. For direct decomposition of carbon monoxide, it is important that the temperature is maintained while the catalyst is in contact with the exhaust gas. Therefore, the catalyst can be provided inside a combustion furnace that can directly contact high-temperature exhaust gas. Specifically, since the activity of the catalyst is the highest within the above temperature range, it is preferable to provide a catalyst at the rear of the combustion furnace because the high-temperature exhaust gas can come into contact with the catalyst when discharged from the combustion furnace.
본 발명의 촉매가 배가스와 접촉할 때의 기체공간속도(GHSV, Gas hourly space velocity)는 500 내지 200,000h-1, 바람직하게 1,000 내지 100,000h-1일 수 있다. 기체공간속도는 유체원료의 공급속도를 장치 부피로 나눈 값으로, 촉매의 유체원료 처리능률을 나타내는 것으로 기체공간속도가 높을수록 처리능률이 높다.Gas hourly space velocity (GHSV) when the catalyst of the present invention contacts exhaust gas may be 500 to 200,000 h -1 , preferably 1,000 to 100,000 h -1 . The gas space velocity is the supply rate of the fluid material divided by the volume of the device, and indicates the catalyst's processing efficiency of the fluid material. The higher the gas space velocity, the higher the processing efficiency.
연소로에서 배출된 배가스는 배기구를 통해 외부로 배기될 수 있다.The exhaust gas discharged from the combustion furnace may be exhausted to the outside through an exhaust port.
따라서, 본 발명의 질소산화물 분해 촉매는 추가적인 가열 과정 없이도 연소로에서 배출되는 배가스의 온도 범위 내에서 활성을 가질 수 있으므로 고온의 가열 공정 없이 대기 오염 물질을 제거할 수 있어 경제적인 장점이 있다.Therefore, the nitrogen oxide decomposition catalyst of the present invention can be active within the temperature range of the exhaust gas discharged from the combustion furnace without an additional heating process, so it can remove air pollutants without a high temperature heating process, which has an economical advantage.
또한, 본 발명의 장치는 연소로에서 배출된 배가스가 외부로 배기되는 경로 상에 팬을 추가적으로 포함할 수 있다. 상기 팬은 배가스의 흐름을 유도할 수 있는 것이라면 제한 없이 사용할 수 있다.In addition, the device of the present invention may additionally include a fan in the path through which the exhaust gas discharged from the combustion furnace is exhausted to the outside. The fan can be used without limitation as long as it can induce the flow of exhaust gas.
따라서, 본 발명의 장치를 이용할 경우 환원제의 사용 및 추가적인 고온 가열 공정 없이도 배가스로부터 질소산화물을 간편하게 저감할 수 있고, 공간적 제약이 적으므로 비교적 소규모의 연소 시설에서도 경제적으로 실시할 수 있다.Therefore, when using the device of the present invention, nitrogen oxides can be easily reduced from exhaust gas without the use of a reducing agent or an additional high-temperature heating process, and because there are few spatial restrictions, it can be economically implemented even in relatively small combustion facilities.
이하, 구체적인 실시예를 통해 본 발명을 보다 구체적으로 설명한다. 하기 실시예는 본 발명의 이해를 돕기 위한 예시에 불과하며, 본 발명의 범위가 이에 한정되는 것은 아니다.Hereinafter, the present invention will be described in more detail through specific examples. The following examples are merely examples to aid understanding of the present invention, and the scope of the present invention is not limited thereto.
실시예Example
촉매의 전환율 평가Catalyst conversion rate evaluation
실시예 1Example 1
일산화질소(NO) 500ppm, 산소(O2) 5%, 수증기(H2O) 4%로 조성된 유사 배가스를 제조하여 촉매의 전환율을 평가하였으며, 이 때 기체공간속도(GHSV, Gas hourly space velocity)는 90,000h-1로 수행하였다.The conversion rate of the catalyst was evaluated by producing a similar exhaust gas composed of 500 ppm nitrogen monoxide (NO), 5% oxygen (O 2 ), and 4% water vapor (H 2 O), and the gas hourly space velocity (GHSV) was evaluated. ) was carried out at 90,000h -1 .
Al2O3 지지체에 Cu를 함유하는 촉매(촉매 1)를 연소로 후단에 설치하고 800 내지 1000℃에서 일산화질소를 산소 및 질소로 전환하는 전환율을 측정하고 도 3에 그 결과를 나타내었다.A catalyst (catalyst 1) containing Cu on an Al 2 O 3 support was installed at the rear of the combustion furnace, and the conversion rate of nitrogen monoxide into oxygen and nitrogen was measured at 800 to 1000°C, and the results are shown in FIG. 3.
도 3에 나타낸 바와 같이, 촉매 1은 900 내지 1000℃ 온도 범위에서 8% 이상의 전환율을 나타내는 것을 확인하여 900℃ 이상의 고온에서도 상기 촉매가 활성을 갖는 것을 확인하였다. As shown in Figure 3, it was confirmed that Catalyst 1 exhibited a conversion rate of 8% or more in the temperature range of 900 to 1000°C, confirming that the catalyst was active even at high temperatures of 900°C or higher.
실시예 2Example 2
CeO2 지지체에 Rh를 함유하는 촉매(촉매 2)를 사용하고, 600 내지 800℃에서 측정한 것을 제외하고 실시예 1과 동일한 조건에서 촉매가 일산화질소를 산소 및 질소로 전환하는 전환율을 측정하고 도 4에 그 결과를 나타내었다.A catalyst (catalyst 2) containing Rh was used on a CeO 2 support, and the conversion rate of the catalyst converting nitrogen monoxide into oxygen and nitrogen was measured under the same conditions as in Example 1, except that the measurement was performed at 600 to 800 ° C. The results are shown in 4.
도 4에 나타낸 바와 같이, 촉매 2는 약 20 내지 30%의 전환율을 나타냈고, 650 내지 800℃ 범위에서 온도가 증가할수록 전환율이 증가하는 경향을 나타냈다.As shown in Figure 4, Catalyst 2 showed a conversion rate of about 20 to 30%, and the conversion rate tended to increase as the temperature increased in the range of 650 to 800°C.
실시예 3Example 3
PrO2 단독 사용 촉매(촉매 3), PrO2 지지체에 Rh를 함유하는 촉매(촉매 4) 및 TiO2 지지체에 Pt를 함유하는 촉매(촉매 5)를 사용하고, 700℃에서 측정한 것을 제외하고 실시예 1과 동일한 조건에서 촉매가 일산화질소를 산소 및 질소로 전환하는 전환율을 측정하고 하기 표 1에 그 결과를 나타내었다.Excluding that a catalyst using only PrO 2 (Catalyst 3), a catalyst containing Rh on a PrO 2 support (Catalyst 4), and a catalyst containing Pt on a TiO 2 support (Catalyst 5) were used and measured at 700°C. The conversion rate at which the catalyst converts nitrogen monoxide into oxygen and nitrogen was measured under the same conditions as in Example 1, and the results are shown in Table 1 below.
상기 표 1에 나타낸 바와 같이, 촉매 3 및 4는 700℃에서 각각 72.4%, 76.7%의 전환율을 나타냈고 촉매 5는 30.4%의 전환율을 나타냈다.As shown in Table 1, Catalysts 3 and 4 showed conversion rates of 72.4% and 76.7%, respectively, at 700°C, and Catalyst 5 showed a conversion rate of 30.4%.
실시예 4Example 4
상기 촉매 4를 사용하여 400 내지 800℃에서 측정한 것을 제외하고 실시예 1과 동일한 조건에서 촉매가 일산화질소를 산소 및 질소로 전환하는 전환율을 측정하고 도 5에 그 결과를 나타내었다.The conversion rate of the catalyst converting nitrogen monoxide into oxygen and nitrogen was measured under the same conditions as in Example 1, except that it was measured at 400 to 800°C using Catalyst 4, and the results are shown in FIG. 5.
도 5에 나타낸 바와 같이, 550 내지 700℃ 온도 범위에서 약 75.9% 내지 91.4%의 우수한 전환율을 나타내는 것을 확인하였다As shown in Figure 5, it was confirmed that an excellent conversion rate of about 75.9% to 91.4% was observed in the temperature range of 550 to 700°C.
이상에서 본 발명의 실시예에 대하여 상세하게 설명하였지만 본 발명의 권리범위는 이에 한정되는 것은 아니고, 청구범위에 기재된 본 발명의 기술적 사상을 벗어나지 않는 범위 내에서 다양한 수정 및 변형이 가능하다는 것은 당 기술분야의 통상의 지식을 가진 자에게는 자명할 것이다.Although the embodiments of the present invention have been described in detail above, the scope of the present invention is not limited thereto, and various modifications and variations are possible without departing from the technical spirit of the present invention as set forth in the claims. This will be self-evident to those with ordinary knowledge in the field.
Claims (3)
상기 연소로 후단에 구비된 일산화질소(NO) 분해 촉매;
를 포함하고,
상기 촉매는 상기 배가스와 접촉하여 일산화질소(NO)를 질소(N2) 및 산소(O2)로 직접 분해하며,
상기 촉매는 금속산화물 지지체에 활성 금속이 담지된 촉매이고,
상기 금속산화물 지지체는 PrO2이고,
상기 활성 금속은 Cu, Pt 및 Rh로 이루어진 그룹에서 선택되는 적어도 하나이며,
상기 배가스는 온도가 550 내지 700℃이고,
상기 배가스가 촉매와 접촉할 때의 기체공간속도(GHSV, Gas hourly space velocity)는 500 내지 200,000h-1인,
질소산화물 저감 장치.A combustion furnace that emits exhaust gases containing nitrogen monoxide (NO); and
A nitrogen monoxide (NO) decomposition catalyst provided at the rear of the combustion furnace;
Including,
The catalyst contacts the exhaust gas and directly decomposes nitrogen monoxide (NO) into nitrogen (N 2 ) and oxygen (O 2 ),
The catalyst is a catalyst in which an active metal is supported on a metal oxide support,
The metal oxide support is PrO 2 ,
The active metal is at least one selected from the group consisting of Cu, Pt and Rh,
The exhaust gas has a temperature of 550 to 700°C,
The gas hourly space velocity (GHSV) when the exhaust gas contacts the catalyst is 500 to 200,000 h -1 ,
Nitrogen oxide reduction device.
상기 활성 금속의 함량은 촉매 전체 중량에 대하여 0 초과 내지 30 중량%인, 질소산화물 저감 장치.According to paragraph 1,
A nitrogen oxide reduction device in which the content of the active metal is greater than 0 to 30% by weight based on the total weight of the catalyst.
팬을 추가로 포함하는, 질소산화물 저감 장치.According to paragraph 1,
A nitrogen oxide reduction device further comprising a fan.
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