US20040168433A1 - Exhaust gas treatment system and exhaust gas treatment method - Google Patents

Exhaust gas treatment system and exhaust gas treatment method Download PDF

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US20040168433A1
US20040168433A1 US10/704,784 US70478403A US2004168433A1 US 20040168433 A1 US20040168433 A1 US 20040168433A1 US 70478403 A US70478403 A US 70478403A US 2004168433 A1 US2004168433 A1 US 2004168433A1
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catalyst
exhaust gas
reducing
gas treatment
denitrifying
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Shigeru Nojima
Kozo Iida
Masashi Kiyosawa
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Mitsubishi Heavy Industries Ltd
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Mitsubishi Heavy Industries Ltd
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Assigned to MITSUBISHI HEAVY INDUSTRIES, LTD. reassignment MITSUBISHI HEAVY INDUSTRIES, LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: IIDA, KOZO B., KIYOSAWA, MASASHI, NOJIMA, SHIGERU
Assigned to MITSUBISHI HEAVY INDUSTRIES, LTD. reassignment MITSUBISHI HEAVY INDUSTRIES, LTD. CORRECTED RECORDATION OF ASSIGNMENT TO CORRECT THE NAME OF NVENTOR "KOZO IIDA Assignors: IIDA, KOZO, KIYOSAWA, MASASHI, NOJIMA, SHIGERU
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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
    • 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
    • B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides

Definitions

  • the present invention relates to an exhaust gas treatment system and an exhaust gas treatment method and, more particularly, to an exhaust gas treatment method in which exhaust gas such as nitrogen oxides and sulfur trioxide (SO 3 ) exhausted from a boiler or the like is removed by reduction using a catalyst.
  • exhaust gas such as nitrogen oxides and sulfur trioxide (SO 3 ) exhausted from a boiler or the like is removed by reduction using a catalyst.
  • a SO 3 reducing reaction using a ruthenium (Ru) carrying catalyst converts sulfur trioxide (SO 3 ) into sulfur dioxide (SO 2 ) using ammonia (NH 3 ) as a reducing agent according to the following reaction formula (1).
  • ruthenium (Ru) carrying catalyst converts sulfur trioxide (SO 3 ) into sulfur dioxide (SO 2 ) using ammonia (NH 3 ) as a reducing agent according to the following reaction formula (1).
  • combustion exhaust gas exhausted from a coal-fired or oil-fired combustion boiler is a gas containing nitrogen oxides.
  • a denitrifier is provided on the downstream side of the combustion boiler so that ammonia (NH 3 ) is injected into the combustion exhaust gas through an injection nozzle to be caused to react with nitrogen oxides (NO, NO 2 ) by reduction, by which the exhaust gas is decomposed into nitrogen (N 2 ) and water (H 2 O), which are harmless.
  • ammonia is usually added to cause sufficient denitrifying reaction.
  • the aforementioned ruthenium (Ru) carrying catalyst not only can remove sulfur trioxide (SO 3 ) by reduction, but also can reduce nitrogen oxides (NOx) in the exhaust gas using ammonia (NH 3 ) according to the following reaction formula (2) to convert them into nitrogen gas (N 2 ).
  • the present invention provides an exhaust gas treatment system for removing nitrogen oxide and sulfur trioxide in exhaust gas by using a catalyst, characterized in that a SO 3 reducing catalyst on the upstream side and a denitrifying catalyst on the downstream side are arranged in series with respect to the flow direction of exhaust gas.
  • the SO 3 reducing catalyst is preferably a catalyst in which Ru is carried as an active metal on a carrier.
  • the carrier used for the SO 3 reducing catalyst preferably contains at least one kind selected from a group consisting of titania, alumina, zirconia, silica, and zeolite.
  • the SO 3 reducing catalyst can contain at least one kind selected from a group consisting of Mo, W and V as a co-catalyst in the carrier.
  • the denitrifying catalyst can use a catalyst that carries at least one kind selected from a group consisting of Mo, W and V as an active metal on a carrier containing titania.
  • the shapes of the SO 3 reducing catalyst and the denitrifying catalyst are not subject to any special restriction, and both of these catalysts can be, for example, a catalyst formed into a honeycomb shape.
  • the present invention provides an exhaust gas treatment method for removing nitrogen oxide and sulfur trioxide in exhaust gas by using a catalyst, characterized in that the treatment method includes a SO 3 reducing process for reducing SO 3 using a SO 3 reducing catalyst on the upstream side and a denitrifying process for removing nitrogen oxides using a denitrifying catalyst on the downstream side with respect to the flow direction of exhaust gas.
  • the treating method in accordance with the present invention preferably includes an NH 3 adding process for adding ammonia NH 3 , which is a reducing agent for nitrogen oxides and SO 3 , in a mole ratio of NH 3 /NOx favorably not lower than the equivalent at the preceding stage of the SO 3 reducing process.
  • the concentration of NH 3 at the downstream outlet of the SO 3 reducing catalyst is preferably 3 ppm or higher in the SO 3 reducing process.
  • NOx and SO 3 can be removed by reduction efficiently at the same time. Therefore, in the exhaust gas treatment using the system in accordance with the present invention, in particular, equipment on the downstream side of the denitrifier is less liable to be deteriorated or damaged, so that this treatment system has an advantage that the maintenance of the whole system is easy and the long-term use is ensured.
  • FIG. 1 are a block diagram showing one example of a system incorporating an exhaust gas treatment system in accordance with the present invention.
  • a SO 3 reducing process is conducted on the upstream side and a denitrifying process is conducted on the downstream side with respect to the flow direction of exhaust gas containing nitrogen oxides.
  • ammonia NH 3 which is a reducing agent for nitrogen oxides and SO 3 in exhaust gas
  • NH 3 adding process ammonia should be added to the exhaust gas in a mole ratio NH 3 /NOx of ammonia to nitrogen oxides NOx preferably not lower than the equivalent (not lower than 1), further preferably not lower than 1.2. Since the concentration of ammonia added to the exhaust gas is high at the preceding stage of the process in which reducing reaction takes place, the SO 3 reducing process is first conducted in a state in which the concentration of ammonia is high.
  • SO 3 is reduced by a SO 3 reducing catalyst, described later.
  • the SO 3 reducing catalyst concurrently carries out three reactions: (1) SO 3 reducing reaction, (2) denitrifying reaction, and (3) NH 3 decomposing reaction.
  • the SO 3 reducing catalyst not only removes sulfur trioxide (SO 3 ) by reduction, but also reduces nitrogen oxides (NOx) in the exhaust gas using ammonia (NH 3 ) to convert into nitrogen gas (N 2 ).
  • the concentration of NH 3 at the downstream outlet of the SO 3 reducing catalyst should preferably be 3 ppm or higher, further preferably be 10 ppm or higher. If the concentration of NH 3 is too low, the reducing agent runs short in a downstream denitrifying process, so that sufficient denitrifying action cannot be brought about.
  • the denitrifying process is conducted.
  • nitrogen oxides are removed using a denitrifying catalyst, described later, according to the following formula (2) or the like.
  • SO 2 oxidizing reaction is produced by a denitrifying catalyst according to the following formula (4), so that the concentration of SO 3 increases further in some cases. For this reason as well, a method in which SO 3 is not yielded in exhaust gas as far as possible is needed. According to the treatment method in accordance with the present invention, SO 3 can be removed effectively on the upstream side of the denitrifying process.
  • the exhaust gas exhausted from the boiler is sent to a denitrifying catalyst, and a denitrifying process is conducted.
  • a denitrifying process ammonia NH 3 added on the upstream side of the denitrifying catalyst is used as a reducing agent.
  • the SO 3 reducing process is usually provided on the upstream side of the denitrifying process, so that denitrification is carried out by using ammonia added at the preceding stage of the SO 3 reducing process.
  • a predetermined quantity of ammonia may be added as necessary at the following stage of the SO 3 reducing process and at the preceding stage of the denitrifying process.
  • both NOx and SO 3 are removed by reduction, and the added NH 3 is also removed after acting as a reducing agent.
  • both NOx and SO 3 are removed by reduction, so that corrosion caused by SO 3 is restrained even if the exhaust gas is caused to pass through the downstream equipment such as a dust collector and a wet type desulfurizer.
  • a heating process using a heater or steam, a dust collecting process using an electric dust collector, a heat recovery process using a gas heater, and the like process are included.
  • FIG. 1 shows one example of an exhaust gas treatment system incorporating an exhaust gas treatment system in accordance with the present invention.
  • the whole of the exhaust gas treatment system in accordance with the embodiment shown in FIG. 1 will be described in detail with reference to the accompanying drawing.
  • a SO 3 reducing catalyst on the upstream side and a denitrifying catalyst on the downstream side are provided in series with respect to the flow direction of exhaust gas containing nitrogen oxides.
  • a SO 3 reducing catalyst 2 on the downstream side of a boiler 1 , a SO 3 reducing catalyst 2, a denitrifier 3 , an air heater (A/H) 4 , which is heating means, a dust collector 5 , a heat exchanger (GGH) 6 for recovering heat energy, a wet type desulfurizer (desulfurizing absorption tower) 7 , a heat exchanger (GGH) 6 for reheating, and a stack 8 are arranged in that order.
  • the SO 3 reducing catalyst 2 is provided on the downstream side of the boiler 1 and on the upstream side of the denitrifier 3 .
  • NH 3 adding means 9 for adding ammonia, which serves as a reducing agent, is provided on the upstream side of the SO 3 reducing catalyst.
  • NH 3 adding means 9 provided on the upstream side of the SO 3 reducing catalyst 2
  • equipment formed by, for example, a reducing agent injection pipe or a plurality of spray nozzles is used.
  • a method for injecting a reducing agent containing ammonia there is available a method in which the reducing agent is vaporized, and the vaporized reducing agent is diluted by adding air, inert gas, water vapor, etc. before the reducing agent is added to the exhaust gas.
  • a plurality of nozzles are arranged perpendicularly to the gas flow.
  • any catalyst can be used if it has a SO 3 reducing function.
  • a catalyst in which Ru is carried as an active metal on a carrier can be cited.
  • the kind of carrier used for the SO 3 reducing catalyst is not subject to any special restriction, but the carrier is preferably at least one kind selected from a group consisting of titania, alumina, zirconia, silica, and zeolite.
  • the SO 3 reducing catalyst can contain at least one kind selected from a group consisting of Mo, W and V as a co-catalyst in the carrier as necessary.
  • the shape of the SO 3 reducing catalyst is not subject to any special restriction.
  • a honeycomb-shaped catalyst a catalyst formed by stacking the honeycomb-shaped catalysts, a catalyst formed by filling particulate catalysts, and the like can be used.
  • a honeycomb-shaped catalyst is preferably used.
  • a denitrifying catalyst used in the denitrifier 3 of this system a catalyst formed by carrying at least one kind selected from a group consisting of Mo, W and V as an active metal on a carrier containing titania can be used preferably.
  • a catalyst in which an active metal of at least one kind selected from a group consisting of Pt, Pd, Ir, Ru, Cu, Co, Fe, Ag, Mn, Ni, Zn and In is contained in the carrier of at least one kind selected from a group consisting of Al 2 O 3 , SiO 2 , ZrO 2 , TiO 2 , metallosilicate, and zeolite can be used.
  • the shape of the nitrifying catalyst is not subject to any special restriction.
  • a honeycomb-shaped catalyst a catalyst formed by stacking the honeycomb-shaped catalysts, a catalyst formed by filling particulate catalysts, and the like can be used.
  • a honeycomb-shaped catalyst is preferably used.
  • the SO 3 reducing catalyst 2 on the upstream side and the denitrifying catalyst system 3 on the downstream side are arranged in series with respect to the flow of exhaust gas.
  • various types of equipment as shown in FIG. 1 are provided according to the treatment of exhaust gas.
  • the air heater (A/H) 4 which is heating means, and the dust collector 5 are provided on the downstream side of the denitrifier 3 .
  • the dust collector 5 is not subject to any special restriction if it can collect dust roughly before the exhaust gas is introduced into the desulfurizing absorption tower 7 .
  • the heat exchanger (GGH) 6 for recovering heat energy and the desulfurizer (desulfurizing absorption tower) 7 are provided on the downstream side of the dust collector 5 .
  • the desulfurizer 7 is not subject to any special restriction.
  • a wet type desulfurizer generally used for flue gas treatment or a desulfurizer in which a cooling tower is provided at the preceding stage of an absorption tower is used.
  • an ordinary wet type desulfurizer can be used.
  • an absorbent used for wet desulfurization aqueous solution of absorbent (alkali absorbent) of calcium carbonate, calcium oxide, calcium hydroxide, sodium carbonate, sodium hydroxide, and the like can be cited.
  • the heat exchanger 6 for reheating is provided on the downstream side of the desulfurizing absorption tower 7 , and the exhaust gas is discharged to the air through the stack 8 after passing through these types of equipment.
  • the combustion exhaust gas whose temperature has been decreased is heated by heat energy recovered by the heat exchanger 6 for heat recovery at the preceding stage of the desulfurizer 7 .
  • the heat exchanger for heat recovery and the heat exchanger for reheating are formed by a gas heater of a system in which heat energy is exchanged by using a heat medium as a medium, and may be a separate system or may be a gas-gas heater for directly effecting heat exchange if they can cool and heat the exhaust gas, respectively.
  • the exhaust gas to be treated by the treatment system in accordance with the present invention is boiler exhaust gas generated in a thermal electric power station, a factory, etc. in which a fuel containing sulfur and mercury, such as coal and heavy oil, is burned or heating furnace exhaust gas generated in a metal factory, an oil refinery, a petrochemical plant, etc.
  • the treatment system in accordance with the present invention is suitable for a large quantity of exhaust gas containing carbon dioxide, oxygen, SOx, soot, or water.
  • Aqueous solution of ruthenium chloride (RuCl 3 ) was impregnated into and carried on particles of compound 1: TiO 2 (MC-90 manufactured by Ishihara Sangyo Kaisha, Ltd.), compound 2: ⁇ -Al 2 O 3 (manufactured by Sumitomo Chemical Co., Ltd.), compound 3: SiO 2 (manufactured by Fuji Silysia Chemical Ltd.), compound 4: zirconia (manufactured by Nikki Chemical Co., Ltd.), compound 5: silicalite (manufactured by Mobil Corp.), compound 6: TiO 2 -WO 3 (weight ratio 90:10), compound 7: TiO 2 -WO 3 (weight ratio 80:20), compound 8: TiO 2 -WO 3 -V 2 O 5 (weight ratio 90:9:1), compound 9: TiO 2 -MoO 3 -V 2 O 5 (weight ratio 90:9:1), and compound 10: TiO 2 -SiO 2 (
  • the powder catalysts 1-10 were put in water, and slurried by ball mill grinding.
  • the slurries 1-10 were applied to and carried on a honeycomb (Ap: 445 m 2 /m 3 ) of TiO 2 -WO 3 (weight ratio 90:10) with a pitch of 7.0 mm and a wall thickness of 1.0 mm in an amount of 200 g/m 2 per honeycomb surface area, by which honeycomb catalysts 1-10 were obtained.
  • a honeycomb catalyst (pitch: 7.0 mm, wall thickness: 1.0 mm, Ap: 445 m 2 /m 3 ) consisting of TiO 2 -WO 3 -V 2 O 5 (weight ratio 91:8.8:0.2) was use
  • Catalyst systems were formed by combining honeycomb catalysts 1-10 (SO 3 reducing catalyst) prepared in example 1 and honeycomb catalyst 11 (denitrifying catalyst) with each other, and exhaust gas treatment tests were conducted under the conditions described below.
  • the gas composition was 150 ppm NOx, 2900 ppm SOx (including 80 ppm SO 3 ), 180 ppm NH 3, 1.3 % O 2 , 10% H 2 O, 10% CO 2 , the balance being N 2 .
  • test conditions were as follows: temperature: 380° C., superficial velocity: 3.3 mN/s, gas quantity: 30 m 3 N/s, catalyst formation: 50 mm square ⁇ 800 mm (preceding stage: one SO 3 reducing catalyst, following stage: one denitrifying catalyst), and GHSV: 15000 h ⁇ 1 at outlet of SO 3 reducing catalyst, 5000 h ⁇ 1 at outlet of denitrifying catalyst (AV: 34 m 3 /m 2 ⁇ h at outlet of SO 3 reducing catalyst, 11 m 3 /m 2 ⁇ h at outlet of denitrifying catalyst).
  • Table 1 gives exhaust gas treatment performance at a total GHSV of 5000 h ⁇ 1 in the case where honeycomb catalysts 1-10 serving as the SO 3 reducing catalyst and honeycomb catalyst 11 serving as the denitrifying catalyst were arranged in series.
  • the concentration of NOx was measured by the chemiluminescence method, the concentration of NH 3 was measured by ion chromatography, and the concentration of SO 3 was measured by arsenazo III method using a spiral tube.
  • the NOx removal efficiency and SO 3 reduction amount were calculated by the following formulae.
  • the target performance of this exhaust gas treatment test was set so as to be a target that satisfies all of the following performances.
  • Honeycomb catalysts 12 and 13 were prepared by the same preparation method as that for SO 3 reducing catalyst 6 (honeycomb catalyst 6) in example 1 except that slurries that carried 0.3% and 1% Ru, in place of 0.5% Ru, on TiO 2 -WO 3 carrier of compound 6 were prepared.
  • honeycomb catalyst 14 was prepared by the same preparation method as that for SO 3 reducing catalyst 6 (honeycomb catalyst 6) in example 1 except that slurry 6 was applied to the honeycomb in an amount of 100 g/m 2 per honeycomb surface area in place of 200 g/m 2 .
  • Exhaust gas treatment tests were conducted in the same way as test 6 in example 2 on catalyst systems in which each one of the honeycomb catalysts 12 , 13 and 14 (SO 3 reducing catalysts) and one denitrifying catalyst 11 were combined with each other. Further, an exhaust gas treatment test (test 14) was conducted in the same way as described above on a catalyst system in which two honeycomb catalysts 6 (SO 3 reducing catalysts) and one denitrifying catalyst 11 were combined with each other.
  • the activity evaluation was carried out under the following test conditions based on the catalyst combination and test conditions of test 6 that had exhibited high performance in the above-described tests on catalyst system.
  • Test 15 . . . An activity evaluation test was conducted by the same method as that of test 6 except that the concentration of NH 3 in the gas at the inlet of catalyst was 153 ppm in place of the 180 ppm in test 6 in example 2.
  • Test 16 . . . An activity evaluation test was conducted by the same method as that of test 6 except that the concentration of SO 3 in the gas at the inlet was 50 ppm in place of the 80 ppm in test 6 in example 2.
  • Test 17 . . . An activity evaluation test was conducted by the same method as that of test 6 except that the concentration of NOx in the gas at the inlet was 170 ppm in place of the 150 ppm in test 6 in example 2.
  • Test 18 . . . An activity evaluation test was conducted by the same method as that of test 6 except that the concentration of O 2 in the gas at the inlet was 2% in place of the 1.3% in test 6 in example 2.
  • Test 19 . . . An activity evaluation test was conducted by the same method as that of test 6 except that the concentration of SOx in the gas at the inlet was 4000 ppm (including 80 ppm of concentration of SO 3 ) in place of the 2900 ppm (including 80 ppm of concentration of SO 3 ) in test 6 in example 2.
  • Table 3 gives the exhaust gas treatment test results in the above-described tests 15 to 19.
  • Table 3 Exhaust gas treatment performance of combined catalysts under each test condition Preceding-stage Following-stage NOx Leak of Changed item of catalyst (SO 3 catalys removal SO 3 reduction NE Test test conditions reducing catalyst) (denitrifying catalyst) efficiency (%) amount (ppm) (ppm) 15 NH 3 Catalyst 6 Catalyst 11 90 4 1 Concentration 153 ppm 16 SO 3 Catalyst 6 Catalyst 11 96 6 8 concentration 50 ppm 17 Nox Catalyst 6 Catalyst 11 91 5 1 concentration 170 ppm 18 O 2 Catalyst 6 Catalyst 11 93 4 3 concentration 2% 19 SOx Catalyst 6 Catalyst 11 95 6 8 concentration 4000 ppm
  • the gas composition was 150 ppm NOx, 2900 ppm SOx (including 80 ppm SO 3 ), 180 ppm NH 3 , 1.3% O 2 , 10% H 2 O, 10% CO 2 , the balance being N 2 .
  • test conditions were as follows: temperature: 380° C., superficial velocity: 3.3 mN/s, gas quantity: 30 m 3 N/s, catalyst formation: 50 mm square ⁇ 800 mm (three SO 3 reducing catalysts), and GHSV: 15000 h ⁇ 1 at outlet of the first SO 3 reducing catalyst, 7500 h ⁇ 1 at outlet of the second one, and 5000 h ⁇ 1 at outlet of the third one (AV: 34 m 3 /m 2 ⁇ h at outlet of the first SO 3 reducing catalyst, 17 m 3 /m 2 h at outlet of the second one, and 11 m 3 /m 2 ⁇ h at outlet of the third one).
  • Table 4 gives the exhaust gas treatment performance results at the catalyst outlet at each GHSV (comparative tests 1, 2 and 3).
  • the SO 3 reducing catalyst be arranged at the preceding stage and the denitrifying catalyst be arranged at the following stage, by which NOx, SO 3 and NH 3 are reduced efficiently.

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Cited By (5)

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US20100192552A1 (en) * 2009-02-04 2010-08-05 Mitsubishi Heavy Industries, Ltd. Exhaust gas treatment catalyst, exhaust gas treatment method, and exhaust gas treatment apparatus
CN102101048A (zh) * 2011-01-25 2011-06-22 清华大学 一种以钛硅复合氧化物为载体的铈基脱硝催化剂及其制备和应用
US20110214624A1 (en) * 2007-09-28 2011-09-08 Steamex Group Ab Method and device for producing a gaseous medium comprising steam
US20130085062A1 (en) * 2011-09-30 2013-04-04 Uchicago Argonne, Llc Novel formulation of hexa-aluminates for reforming fuels
CN114618274A (zh) * 2022-02-21 2022-06-14 柳州钢铁股份有限公司 防止金属换热器腐蚀的方法

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JP4683624B2 (ja) * 2005-05-11 2011-05-18 株式会社四国総合研究所 三酸化硫黄濃度連続測定方法および装置
JP5748894B1 (ja) * 2014-11-07 2015-07-15 三菱重工業株式会社 排ガス処理方法及び脱硝・ｓｏ３還元装置
JP5748895B1 (ja) * 2014-11-07 2015-07-15 三菱日立パワーシステムズ株式会社 排ガス処理システム及び処理方法

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110214624A1 (en) * 2007-09-28 2011-09-08 Steamex Group Ab Method and device for producing a gaseous medium comprising steam
US10006626B2 (en) 2007-09-28 2018-06-26 Steamex Group Sverige Ab Method and device for producing a gaseous medium comprising steam
US10775038B2 (en) 2007-09-28 2020-09-15 Steamex Group Sverige Ab Method and device for producing a gaseous medium comprising steam
US20100192552A1 (en) * 2009-02-04 2010-08-05 Mitsubishi Heavy Industries, Ltd. Exhaust gas treatment catalyst, exhaust gas treatment method, and exhaust gas treatment apparatus
US8910468B2 (en) * 2009-02-04 2014-12-16 Mitsubishi Heavy Industries, Ltd. Exhaust gas treatment catalyst, exhaust gas treatment method, and exhaust gas treatment apparatus
CN102101048A (zh) * 2011-01-25 2011-06-22 清华大学 一种以钛硅复合氧化物为载体的铈基脱硝催化剂及其制备和应用
US20130085062A1 (en) * 2011-09-30 2013-04-04 Uchicago Argonne, Llc Novel formulation of hexa-aluminates for reforming fuels
CN114618274A (zh) * 2022-02-21 2022-06-14 柳州钢铁股份有限公司 防止金属换热器腐蚀的方法

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