WO2016072110A1 - 排ガス処理方法及び脱硝・so3還元装置 - Google Patents
排ガス処理方法及び脱硝・so3還元装置 Download PDFInfo
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- WO2016072110A1 WO2016072110A1 PCT/JP2015/067449 JP2015067449W WO2016072110A1 WO 2016072110 A1 WO2016072110 A1 WO 2016072110A1 JP 2015067449 W JP2015067449 W JP 2015067449W WO 2016072110 A1 WO2016072110 A1 WO 2016072110A1
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- Prior art keywords
- exhaust gas
- catalyst
- denitration
- reduction
- catalyst layer
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Definitions
- the present invention relates to an exhaust gas treatment method and a denitration / SO 3 reduction device, and more particularly to an exhaust gas treatment method and a denitration / SO 3 reduction device for combustion exhaust gas containing sulfur trioxide.
- the present invention provides an exhaust gas treatment method and a denitration / SO 3 reduction device that lower the processing cost than before, reduce NO x in combustion exhaust gas, and reduce the SO 3 concentration. With the goal.
- an exhaust gas treatment method adds a compound containing H element and C element as a first additive to combustion exhaust gas containing SO 3 in addition to NO X , and then Ti.
- a catalyst containing, as a support one or more oxides of an element selected from the group consisting of Si, Zr and Ce and / or a mixed oxide and / or composite oxide of two or more elements selected from the group SO 3 is reduced to SO 2 .
- the first additive includes olefinic hydrocarbons having 2 to 5 carbon atoms (unsaturated hydrocarbons), paraffinic hydrocarbons having 2 to 5 carbon atoms (saturated hydrocarbons), alcohols, aldehydes, and aromatic compounds It is suitable that it is 1 or more types chosen from the group which consists of. Further, the olefinic hydrocarbon having 2 to 5 carbon atoms (unsaturated hydrocarbon) is at least one selected from the group consisting of C 2 H 4 , C 3 H 6 , C 4 H 8 and C 5 H 10 . Those are preferred. The C 4 H 8 and C 5 H 10 may be any one of geometric isomers or racemates.
- the carrier is preferably one or more mixed oxides and / or complex oxides selected from the group consisting of TiO 2 —SiO 2 , TiO 2 —ZrO 2 and TiO 2 —CeO 2 .
- mixed oxide and / or composite oxide with TiO 2 can be used, and the reduction performance of SO 3 to SO 2 can be drastically improved with a solid acid amount of a predetermined value or more. .
- the catalyst may be V 2 O 5 , WO 3 , MoO 3 , Mn 2 O 3 , MnO 2 with one or more selected from the group consisting of the oxide, the mixed oxide and the composite oxide as a support.
- NiO and Co 3 O 4 can be used as a catalyst carrying one or more metal oxides selected from the group consisting of NiO and Co 3 O 4 .
- the catalyst includes at least one selected from the group consisting of Ag, Ag 2 O, and AgO, with one or more selected from the group consisting of the oxide, the mixed oxide, and the composite oxide as a support.
- a supported catalyst can also be used.
- the catalyst includes a metallosilicate complex oxide in which at least a part of Al and / or Si in the zeolite crystal structure is substituted with one or more selected from the group consisting of Ti, V, Mn, Fe and C Firm. Can be coated or impregnated.
- the first additive can be added simultaneously by some modification of the ammonia supply line equipment incidental to existing denitration apparatus, it is possible to contribute to a reduction in SO 3 in the combustion exhaust gas .
- the treatment for reducing SO 3 to SO 2 is preferably performed within a temperature range of 250 ° C. to 450 ° C. Further, the treatment for reducing SO 3 to SO 2 is more preferably performed within a temperature range of 300 ° C. or more and 400 ° C. or less.
- the present invention is a denitration / SO 3 reduction device in another aspect.
- a denitration / SO 3 reduction device according to the present invention is provided near a first injection device for adding a first additive to combustion exhaust gas containing SO 3 in addition to NO X , and the first injection device.
- the catalyst is one or more oxides of elements selected from the group consisting of Ti, Si, Zr and Ce and / or two or more mixed oxides of elements selected from the group and / or A composite oxide is used as a support.
- the catalyst layer is a first catalyst layer that reduces the SO 3 concentration disposed downstream of the first injection device, and denitration disposed downstream of the second injection device.
- the first catalyst layer can be arranged in the upstream or downstream of the second catalyst layer.
- an exhaust gas treatment method and a denitration / SO 3 reduction device that lower the processing cost than before, denitrate NO x in combustion exhaust gas, and lower the SO 3 concentration.
- FIG. 1 is a schematic diagram for explaining a first embodiment of a denitration / SO 3 reduction apparatus according to the present invention.
- FIG. 2 is a schematic diagram for explaining a second embodiment of the denitration / SO 3 reduction device according to the present invention.
- FIG. 3 is a schematic view for explaining a third embodiment of the denitration / SO 3 reduction device according to the present invention.
- FIG. 4 is a graph showing changes in the SO 3 concentration in the combustion exhaust gas for Example 1 according to the present invention.
- FIG. 5 is a graph showing changes in SO 3 concentration in the combustion exhaust gas in Example 2 according to the present invention.
- FIG. 6 is a graph showing the SO 3 reduction rate and the denitration rate in the combustion exhaust gas for Example 2 according to the present invention.
- FIG. 1 is a schematic diagram for explaining a first embodiment of a denitration / SO 3 reduction apparatus according to the present invention.
- FIG. 2 is a schematic diagram for explaining a second embodiment of the denitration / SO 3 reduction device according
- FIG. 7 is a graph showing the SO 3 reduction rate and the denitration rate by the catalyst for Example 3 according to the present invention.
- FIG. 8 is a graph showing the relationship between the amount of solid acid and the SO 3 reduction rate for Example 3 according to the present invention.
- FIG. 9 is a graph showing the SO 3 reduction rate and the denitration rate by the catalyst for Example 4 according to the present invention.
- FIG. 10 is a graph showing the SO 3 reduction rate by the catalyst for Example 5 according to the present invention.
- FIG. 11 is a graph showing the denitration rate by a catalyst in Example 5 according to the present invention.
- combustion exhaust gas an exhaust gas in an oxidizing atmosphere in which petroleum or coal-derived fuel is burned by a boiler.
- combustion exhaust gas an exhaust gas in an oxidizing atmosphere in which petroleum or coal-derived fuel is burned by a boiler.
- the flow direction of the combustion exhaust gas is expressed as a front flow or a back flow.
- FIG. 1 shows a first embodiment in which a denitration / SO 3 reduction device according to the present invention is arranged in the downstream of a boiler.
- a denitration / SO 3 reduction device 5 shown in FIG. 1 is provided downstream of a flue gas flue 2 of a boiler that generates combustion exhaust gas in a furnace 1.
- the boiler burns fuel supplied from the outside in the furnace 1 and discharges the combustion exhaust gas generated by the combustion into the exhaust gas flue 2. Against the flue gas flowing through the exhaust gas flue 2, performed by denitration ⁇ SO 3 reduction device 5 provided on the downstream of the flue 2, reduction of the denitration and SO 3 of the NO X at the same time.
- the main processing for reducing SO 3 to SO 2 is also referred to as SO 3 reduction processing.
- the ECO 3 provided in the exhaust gas flue 2 through which the combustion exhaust gas circulates exchanges heat between the boiler feed water and the combustion exhaust gas that circulates in the inside. That is, the combustion efficiency of a boiler is improved by raising the feed water temperature to a boiler using the residual heat of combustion exhaust gas.
- One end of the ECO bypass 4 communicates with the upstream of the ECO 3 and the other end communicates with the downstream of the ECO 3.
- the combustion exhaust gas before being supplied to the ECO 3 bypasses the ECO 3 and is denitrated and SO 3 reducing device 5. Supplied to the inlet side.
- the ECO bypass 4 controls the temperature of the combustion exhaust gas supplied to the denitration / SO 3 reduction device 5 within a predetermined temperature range suitable for the denitration / reduction reaction.
- the denitration / SO 3 reduction device 5 is provided in the exhaust gas flue 2 and includes at least a first injection device 6, a second injection device 7, and a catalyst layer 8.
- the denitration / SO 3 reduction device 5 adds the first additive and the second additive to the combustion exhaust gas, and allows the combustion exhaust gas to which the additive is added to pass through the catalyst layer 8.
- the denitration / SO 3 reduction device 5 performs SO 3 reduction treatment using the catalyst layer 8, the first injection device 6, and the second injection device 7. Further, the denitration / SO 3 reduction device 5 is preferably configured to simultaneously add the first additive and the second additive.
- the first injection device 6 is arranged upstream of the denitration / SO 3 reduction device 5 and downstream of the ECO bypass 4 and adds the first additive to the combustion exhaust gas containing SO 3 in addition to NO X. . That is, the first injection device 6 cooperates with the catalyst layer 8 to reduce SO 3 in the combustion exhaust gas.
- the first additive injected from the first injection device 6 is an SO 3 reducing agent mainly for reducing SO 3 to SO 2 , and is a carbon element having SO 3 reducing ability in an oxygen atmosphere. Hydrocarbons composed of (C) and / or elemental hydrogen (H) can be used.
- the first additive is an olefinic hydrocarbon (unsaturated hydrocarbon) represented by the general formula: C n H 2n (n is an integer of 2 to 5), the general formula: C m H 2m + 2 (M is an integer of 2 to 5) paraffinic hydrocarbons (saturated hydrocarbons), alcohols such as methanol (CH 3 OH), ethanol (C 2 H 5 OH), acetaldehyde (CH 3 CHO), propion
- aldehydes such as aldehyde (C 2 H 5 CHO)
- aromatic compounds such as toluene (C 6 H 5 CH 3 ) and ethylbenzene (C 6 H 5 C 2 H 5 ) It is an agent.
- the olefinic hydrocarbon having 2 to 5 carbon atoms is preferably at least one selected from the group consisting of C 2 H 4 , C 3 H 6 , C 4 H 8 and C 5 H 10.
- One or more selected from the group consisting of C 3 H 6 , C 4 H 8 and C 5 H 10 having 3 or more carbon atoms is more preferred.
- the C 4 H 8 and C 5 H 10 may be any one of geometric isomers or racemates.
- Examples of the unsaturated hydrocarbon having 4 or more carbon atoms include 2-butene (2-C 4 H 8 ) such as 1-butene (1-C 4 H 8 ), cis-2-butene, and trans-2-butene.
- 2-pentene (2-C 5 H 10 ) such as isobutene (iso-C 4 H 8 ), 1-pentene (1-C 5 H 10 ), cis-2-pentene, trans-2-pentene, etc. .
- 2-pentene (2-C 5 H 10 ) such as isobutene (iso-C 4 H 8 ), 1-pentene (1-C 5 H 10 ), cis-2-pentene, trans-2-pentene, etc.
- it can greatly contribute to the reduction of SO 3 under an excess atmosphere of oxygen, and the SO 3 concentration in the combustion exhaust gas can be lowered.
- the amount of the first additive added is preferably 0.1 to 2.0 in terms of the molar ratio of C 3 H 6 / SO 3 . If it is less than 0.1, the oxidation of SO 2 becomes dominant and SO 3 may increase. If it exceeds 2.0, excessive C 3 H 6 may be discharged in a large amount without being reacted. is there. Within the above range, it is possible to improve the SO 3 removal performance in the combustion exhaust gas. Note that there is an effect of removing SO 3 even outside the specified range.
- the second injection device 7 is arranged close to the first injection device 6 and adds NH 3 as a second additive to the combustion exhaust gas. Second injection device 7 is disposed on the upstream and Wake of ECO bypass 4 denitration ⁇ SO 3 reduction device 5 injects the second additive to denitration the NO X in the flue gas. Second injection device 7 denitrating NO X in cooperation with the catalyst layer 8.
- the catalyst layer 8 is made of a catalyst for denitrating combustion exhaust gas.
- the shape of the catalyst arranged in the catalyst layer 8 is preferably a honeycomb shape in order to function efficiently as a denitration catalyst and to reduce pressure loss in the combustion exhaust gas treatment.
- the honeycomb structure is not limited to a rectangular cross section, and may have a cross section such as a circle, an ellipse, a triangle, a pentagon, and a hexagon.
- the catalyst arranged in the catalyst layer 8 is a catalyst supporting an active component using an oxide, a mixed oxide and / or a composite oxide as a carrier.
- the carrier includes one or more oxides of elements selected from the group consisting of titanium (Ti), silicon (Si), zirconium (Zr), and cerium (Ce) and / or from the group. Two or more mixed oxides and / or complex oxides of the selected elements may be mentioned. That is, the carrier includes at least the following forms.
- the composite oxide can be prepared by mixing an alkoxide compound, chloride, sulfate or acetate, further mixing with water, stirring in an aqueous solution or sol state, and hydrolyzing. Further, the composite oxide may be prepared by a known coprecipitation method other than the sol-gel method described above.
- the active ingredients include vanadia (V 2 O 5 ), tungsten oxide (WO 3 ), molybdenum oxide (MoO 3 ), manganese oxide (Mn 2 O 3 ), manganese dioxide (MnO 2 ), nickel oxide (NiO) and oxidation.
- the active ingredient may be one or more selected from the group consisting of silver (Ag), silver oxide (Ag 2 O), and silver monoxide (AgO).
- the active metal supported on the catalyst serves as an active point, and NO X such as NO and NO 2 can be efficiently denitrated in the presence of oxygen, and the SO 3 in the combustion exhaust gas can be removed in an excess atmosphere of oxygen. Allows reduction.
- the active ingredient preferably contains tungsten oxide (WO 3 ).
- At least a part of aluminum element (Al) and / or silicon element (Si) in the zeolite crystal structure is composed of titanium element (Ti), vanadium element (V), manganese element (Mn), iron.
- Ti titanium element
- V vanadium element
- Mn manganese element
- What coated or impregnated the metallosilicate system complex oxide substituted by 1 or more sorts chosen from the group which consists of an element (Fe) and cobalt element (C Cincinnati) can also be used.
- Such a metallosilicate is prepared, for example, by mixing water glass as a silicon source and at least part of the silicon element with a metal element source to be substituted and a structure indicator, and charging the mixture in an autoclave. It can be prepared by using.
- exhaust gas treatment method The first embodiment of the exhaust gas treatment method according to the present invention will be described by describing the operation mode of the denitration / SO 3 reduction device according to the first embodiment.
- the exhaust gas treatment method of the present embodiment performs at least SO 3 reduction treatment.
- the SO 3 reduction treatment is preferably performed within a temperature range of 250 ° C. or higher and 450 ° C. or lower, and more preferably performed within a temperature range of 300 ° C. or higher and 400 ° C. or lower. If it is lower than 300 ° C., the denitration treatment may be insufficient, and if it exceeds 400 ° C., the reduction of SO 3 may be insufficient due to self-decomposition of the first additive.
- the SO 3 concentration during the treatment of combustion exhaust gas can be reduced, and the material cost of the catalyst can be suppressed without using an expensive catalyst.
- the denitration / SO 3 reduction device 15 according to the present embodiment is the first embodiment in that the catalyst layer is divided into first and second catalyst layers, and the first injection device is disposed between them. This is different from the denitration / SO 3 reduction device 5.
- the denitration / SO 3 reduction device 15 shown in FIG. 2 is provided in the exhaust gas flue 2 and adds a first additive 16 for adding the first additive to the combustion exhaust gas, and a second additive to the combustion exhaust gas.
- a second injection device 17 that performs the denitration of the combustion exhaust gas.
- the catalyst layer includes a first catalyst layer 18 that reduces the SO 3 concentration, and a second catalyst layer 19 that is disposed upstream of the first catalyst layer 18 and performs denitration.
- the denitration / SO 3 reduction device 15 adds the second additive from the second injection device 17 to the combustion exhaust gas flowing from the exhaust gas flue 2, and then passes the second catalyst layer 19.
- the denitration / SO 3 reduction device 15 adds the first additive from the first injection device 16 to the combustion exhaust gas that has passed through the second catalyst layer 19, and then passes the first catalyst layer 18. .
- the first injection device 16 is disposed upstream of the first catalyst layer 18 and downstream of the second catalyst layer 19 in the exhaust gas flue 2.
- the first catalyst layer 18 is disposed downstream of the second catalyst layer 19. Further, the first injection unit 16, to the flue gas, injecting a first additive for reducing the SO 3 concentration.
- the second injection device 17 is arranged upstream of the second catalyst layer 19 in the exhaust gas flue 2.
- the second injection unit 17 injects against flue gas, a second additive for denitrating NO X.
- the denitration apparatus provided in the existing plant is employable, for example.
- the same ones as in the first embodiment can be applied.
- the second additive injected from the second injection device 17 and the catalyst provided in the second catalyst layer 19 are the same as those in the first embodiment, and a known denitration catalyst (for example, V 2). O 5 -TiO 2 ) can also be applied.
- exhaust gas treatment method The second embodiment of the exhaust gas treatment method according to the present invention will be described by describing the operation mode of the denitration / SO 3 reduction device according to the second embodiment.
- the exhaust gas treatment method of the present embodiment performs at least SO 3 reduction treatment.
- NH 3 as the second additive is added to the combustion exhaust gas from the second injection device 17 as a pretreatment for the combustion exhaust gas containing at least NO X and SO 3, and then The denitration catalyst is brought into contact with the combustion exhaust gas at the second catalyst layer 19 provided in the flow. Thereafter, the workup, the SO 3 additive than the first injection device 16 is added to the flue gas, it causes in a first catalyst layer 18 provided on the subsequent flow into contact with the combustion exhaust gas to the catalyst for SO 3.
- the same temperature range as in the first embodiment can be adopted as the processing temperature for the SO 3 reduction treatment.
- the denitration / SO 3 reduction device and the exhaust gas treatment method according to the second embodiment it becomes possible to treat SO 3 more efficiently on the downstream side of the existing denitration device, as well as denitration / SO 3. Catalyst exchange corresponding to the reduction of the respective catalytic functions of reduction is facilitated.
- the denitration / SO 3 reduction device 25 according to the present embodiment is the second in that the first injection device and the first catalyst layer are arranged upstream of the second injection device and the second catalyst layer. This is different from the denitration / SO 3 reduction device 15 of the embodiment.
- a denitration / SO 3 reduction device 25 shown in FIG. 3 is provided in the exhaust gas flue 2, and includes a first injection device 26, a second injection device 27, a first catalyst layer 28, and a second catalyst layer. 29 at least.
- the denitration / SO 3 reduction device 25 adds the second additive from the first injection device 26 to the combustion exhaust gas flowing in from the exhaust gas flue 2 and then passes the first catalyst layer 28. Further, the denitration / SO 3 reduction device 25 adds the second additive from the second injection device 27 to the combustion exhaust gas that has passed through the first catalyst layer 28, and then allows the second catalyst layer 29 to pass through. .
- the first injection device 26 is disposed upstream of the first catalyst layer 28 and upstream of the second catalyst layer 29 in the exhaust gas flue 2.
- the first catalyst layer 28 is disposed upstream of the second catalyst layer 29.
- the first injection device 26 injects a first additive for reducing the SO 3 concentration into the combustion exhaust gas.
- the second injection device 27 is disposed upstream of the second catalyst layer 29 in the exhaust gas flue 2.
- the second injection unit 27 injects against flue gas, a second additive for denitrating NO X. Note that a denitration device provided in an existing plant can be applied to the second injection device 27 and the second catalyst layer 29 as in the second embodiment.
- the same ones as in the first and second embodiments can be applied.
- the second additive injected from the second injection device 27 and the catalyst provided in the second catalyst layer 29 are also known denitration catalysts (for example, V 2) in addition to those similar to the first embodiment. O 5 -TiO 2 ) can also be applied.
- exhaust gas treatment method the third embodiment of the exhaust gas treatment method according to the present invention will be described by explaining the operation mode of the denitration / SO 3 reduction device according to the third embodiment.
- the exhaust gas treatment method of the present embodiment performs at least SO 3 reduction treatment.
- an additive for SO 3 was added to the combustion exhaust gas from the first injection device 26 and provided downstream.
- the SO 3 catalyst is brought into contact with the combustion exhaust gas.
- NH 3 is added as a second additive from the second injection device 27 to the combustion exhaust gas, and the denitration catalyst is brought into contact with the combustion exhaust gas in the second catalyst layer 29 provided downstream.
- the same temperature range as in the first and second embodiments can be adopted as the treatment temperature for the SO 3 reduction treatment.
- the denitration / SO 3 reduction device and the exhaust gas treatment method according to the third embodiment it becomes possible to treat SO 3 more efficiently on the downstream side of the existing denitration device, as well as denitration / SO 3. Catalyst exchange corresponding to the reduction of the catalytic function of each reduction is facilitated.
- Example 1 By changing the catalyst, the effect of reducing SO 3 to SO 2 by the first additive (SO 3 reducing agent) was examined.
- Catalyst A containing Ru (ruthenium) that also functions as a catalyst for reducing SO 3 to SO 2 was prepared.
- Ru ruthenium
- an anatase-type titania powder containing 10 wt% tungsten oxide (WO 3 ) per 100 wt% titania (TiO 2 ) with an aqueous ruthenium chloride (RuCl 3 ) solution 100 wt% anatase titania powder Per 1 wt% of Ru was supported on the powder, evaporated and dried. Thereafter, calcination was carried out at 500 ° C. for 5 hours, and the obtained powder was used as catalyst A.
- Catalyst B was prepared as a typical catalyst having a denitration function with ammonia.
- Ti (O—iC 3 H 7 ) 4 that is a Ti alkoxide and Si (OCH 3 ) 3 that is a Si alkoxide are mixed at a weight ratio of 95: 5 (as TiO 2 and SiO 2 , respectively), and 80 ° C.
- the sol produced by stirring and aging was filtered, and the resulting gelled product was washed, dried, and then heated and fired at 500 ° C. for 5 hours to obtain powdered TiO 2. give -SiO 2 composite oxide (TiO 2 -SiO 2 powder).
- a representative catalyst C having a denitration function with ammonia was prepared.
- Ti (O—iC 3 H 7 ) 4 that is a Ti alkoxide and Zr (Oi—C 4 H 9 ) 4 that is a Zr alkoxide are mixed at a wt% ratio of 95: 5 (as TiO 2 and ZrO 2 , respectively).
- it is hydrolyzed by adding to water at 80 ° C., and then the sol formed by stirring and aging is filtered, and the resulting gelled product is washed, dried, heated and fired at 500 ° C. for 5 hours, A TiO 2 —ZrO 2 composite oxide (TiO 2 —ZrO 2 powder) was obtained.
- ammonium paratungstate the ((NH 4) 10 H 10 W 12 O 46 ⁇ 6H 2 O) was impregnated with 10 wt% aqueous methylamine solution, composite oxide per 100 wt%, the WO 3 8 wt% was supported, evaporated to dryness, and then fired at 500 ° C. for 5 hours.
- the obtained powder was designated as Catalyst C.
- Catalyst D with only titania (TiO 2 ) was prepared.
- Anatase-type titania powder in the same amount as catalyst A was calcined at 500 ° C. for 5 hours to prepare powdered catalyst D.
- Test Examples 1 to 5 80 wt% of water was added to 20 wt% of each of the catalysts A to D, and wet ball milling was performed to obtain a wash coat slurry. Subsequently, a cordierite monolith substrate (7.4 mm pitch, wall thickness 0.6 mm) was dip-coated on the slurry, dried at 120 ° C., and then fired at 500 ° C. The coating amount was 100 g per 1 m 2 of the substrate surface area. Test Example 1 was conducted when Catalyst A was used and ammonia (NH 3 ) was used as the SO 3 reducing agent.
- NH 3 ammonia
- Test Example 2 was performed using Catalyst A and propylene (C 3 H 6 ) as the SO 3 reducing agent.
- Test Example 3 was performed using Catalyst B and C 3 H 6 as the SO 3 reducing agent.
- Test Example 4 was conducted using Catalyst C and C 3 H 6 as the SO 3 reducing agent.
- Test Example 5 was conducted using Catalyst D and C 3 H 6 as the SO 3 reducing agent.
- FIG. 4 shows the change in SO 3 concentration (ppm) relative to 0.03 to 0.08 m 2 ⁇ h / Nm 3 in Test Examples 1 to 5.
- the SO 3 concentration with respect to the catalyst layer inlet hardly changed.
- the SO 3 concentration at the catalyst layer inlet decreased from about 100 ppm to about 40 ppm at 0.06 m 2 ⁇ h / Nm 3 .
- the SO 3 concentration at the catalyst layer inlet decreased from about 100 ppm to about 20 ppm at 0.08 m 2 ⁇ h / Nm 3 .
- the SO 3 concentration at the catalyst layer inlet decreased from about 100 ppm to about 20 ppm at 0.08 m 2 ⁇ h / Nm 3 . Also in Test Example 5, the SO 3 concentration at the catalyst layer inlet decreased from about 100 ppm to about 25 ppm at 0.08 m 2 ⁇ h / Nm 3 .
- Test Example 1 using Ru-containing catalyst A and NH 3 as the SO 3 reducing agent, it was found that the SO 3 concentration with respect to the catalyst layer inlet hardly changed.
- Test Example 2 using Ru-containing catalyst A and C 3 H 6 as the SO 3 reducing agent, it was found that the SO 3 concentration in the combustion exhaust gas decreased.
- Test Example 3 using the expensive catalyst B containing no Ru, it was found that the use of C 3 H 6 as the SO 3 reducing agent significantly reduces the SO 3 concentration in the combustion exhaust gas.
- Test Example 4 using the catalyst C it was found that if C 3 H 6 was used as the SO 3 reducing agent, the SO 3 concentration in the combustion exhaust gas was significantly reduced.
- Example 2 Hydrocarbons having different compositions were used as the first additive (SO 3 reducing agent), and the reduction effect of SO 3 on SO 2 due to the composition of the hydrocarbon compound was examined.
- Example 10 (Preparation of Test Examples 6 to 10) Catalyst B was coated on a cordierite monolith substrate in the same manner as in Example 1. The coating amount was 100 g per 1 m 2 of the substrate surface area.
- the case where C 3 H 6 is used as the SO 3 reducing agent is set as Test Example 6, the case where propane (C 3 H 8 ) is used is set as Test Example 7, and the case where methanol (CH 3 OH) is used is set as Test Example 8. And Example 9 was used when ethanol (C 2 H 5 OH) was used.
- the test example 10 was a case where ammonia (NH 3 ) was used as the SO 3 reducing agent.
- FIG. 5 shows the change in the SO 3 concentration (ppm) in the combustion exhaust gas with respect to 0.04 to 0.08 m 2 ⁇ h / Nm 3 in Test Examples 6 to 10.
- the concentration of SO 3 in the combustion exhaust gas with respect to the catalyst layer inlet decreased.
- Test Example 10 a decrease in SO 3 concentration in the combustion exhaust gas with respect to the catalyst layer inlet was not confirmed.
- Test Examples 5 and 6 using C 3 H 6 and C 3 H 8 as SO 3 reducing agents are more combustible than Test Examples 8 and 9 using CH 3 OH and C 2 H 5 OH as SO 3 reducing agents.
- the SO 3 concentration in the exhaust gas decreased.
- Test Example 6 using C 3 H 6 as the SO 3 reducing agent showed the most remarkable effect of reducing the SO 3 concentration.
- Catalyst E was coated on a cordierite monolith substrate in the same manner as in Example 1.
- the case of using methanol (CH 3 OH) as the SO 3 reducing agent is set as Test Example 11
- the case of using ethanol (C 2 H 5 OH) is set as Test Example 12
- propane (C 3 H 8 ) is used.
- the case of using was designated as Test Example 13.
- FIG. 6 shows the reduction rate (%) and the denitration rate (%) of SO 3 with respect to 0.080 m 2 ⁇ h / Nm 3 in Test Examples 11 to 18.
- the SO 3 reduction rate of Test Example 11 using alcohols was 5.0%
- the SO 3 reduction rate of Test Example 12 was 6.0%
- the SO 3 reduction rate of Test Example 13 using saturated hydrocarbon or unsaturated hydrocarbon is 10.0%
- the SO 3 reduction rate of Test Example 14 is 20.0%, which is a high value. showed that.
- the SO 3 reduction rate of Test Example 15 using an unsaturated hydrocarbon having 3 or more carbon atoms is 58.0%
- the SO 3 reduction rate of Test Example 16 is 50.2%
- the SO 3 reduction rate was 54.2%
- the SO 3 reduction rate of Test Example 18 was 63.5%, indicating a very high value.
- test Example 11 using alcohols was 92.6%, and the denitration rate in Test Example 12 was 93.2%.
- the denitration rate of Test Example 13 using saturated hydrocarbons or unsaturated hydrocarbons was 94.1%, and the denitration rate of Test Example 14 was 94.0%, indicating a high value.
- Test Example 15 using unsaturated hydrocarbons having 3 or more carbon atoms is 95.1%, Test Example 16 is 92.1%, Test Example 17 is 92.3%, Test Example 18 was 91.8%, showing a sufficiently high value.
- Example 3 Further, a catalyst having another composition was prepared, and the reduction effect of SO 3 to SO 2 and the denitration effect by the catalyst composition were examined.
- catalyst G A zirconia (ZrO 2 ) only catalyst was prepared.
- Zirconium oxychloride (ZrOCl 2 ) powder was calcined at 500 ° C. for 5 hours, and the obtained powder was used as catalyst G.
- catalyst H A catalyst containing only cerium oxide (Ce 2 O 3 ) was prepared. Cerium nitrate (Ce (NO 3 ) 2 ) powder was calcined at 500 ° C. for 5 hours, and the obtained powder was used as catalyst H.
- Test Examples 19 to 24 Catalyst D, TiO 2 -SiO 2 powder B, TiO 2 -ZrO 2 powder C, F, for each 20 wt% of G and H, respectively, the water 80 wt% was added, subjected to wet ball milling, the washcoat Then, a ceramic base material mainly composed of kaolinite was coated, and Test Examples 19 to 24 were made.
- the composition of each test example is shown in Table 1. In the table, the average value obtained by measuring two samples using the value obtained by dividing the carrying amount obtained from the weight difference before and after the coating by the surface area of the substrate was used as the average value of the coating amount.
- FIG. 7 shows the reduction rate (%) and denitration rate (%) of SO 3 with respect to 0.080 m 2 ⁇ h / Nm 3 in Test Examples 19 to 24.
- the SO 3 reduction rate of Test Example 19 using a single-component oxide is 16.5%
- the SO 3 reduction rate of Test Example 23 is 23.1%
- the Test Example The SO 3 reduction rate of 24 was 11.1%.
- the SO 3 reduction rate of Test Example 20 using the composite oxide containing TiO 2 was 52.2%
- the SO 3 reduction rate of Test Example 21 was 47.3%
- the SO 3 reduction rate of Test Example 22 was 3 The reduction rate was 46.6%.
- the NOx removal rate of Test Example 19 using a single component oxide is 32.8%
- the NOx removal rate of Test Example 23 is 6.7%
- the NOx removal rate of Test Example 24 is 19.1%. Met.
- the NOx removal rate of Test Examples 20 to 22 using a composite oxide containing TiO 2 is 60.4%
- the NOx removal rate of Test Example 21 is 39.3%
- the NOx removal rate of Test Example 22 is It was 42.3%.
- Test examples 20 to 22 using TiO 2 -SiO 2 powder, TiO 2 -ZrO 2 powder or TiO 2 -Ce 2 O 3 powder are test examples using TiO 2 powder, ZrO 2 powder or Ce 2 O 3 powder.
- the reduction rate of SO 3 was higher than 19 and 23-24.
- Test Examples 19 and 23 to 24 using a single component oxide the reduction rate of Test Example 19 using TiO 2 powder is high, and the reduction rate of Test Example 23 using ZrO 2 powder is the highest. It was.
- Test Example 19 using TiO 2 —SiO 2 powder showed the most remarkable SO 3 reduction rate. From these results, it was found that the reduction rate of SO 3 was high by using a composite oxide, particularly a composite oxide containing TiO 2 . The above results were presumed to be due to the increase in the amount of solid acid due to the composite oxide.
- Test Examples 19 to 24 were measured by the pyridine temperature-programmed adsorption desorption method. More specifically, 25 mg of each test example of the same amount of quartz powder was added and fixed to a quartz glass tube with kao wool. The quartz glass tube was installed in an electric furnace provided for FID gas chromatography, and then treated in a helium (He) stream at a temperature of 450 ° C. for 30 minutes. Thereafter, while maintaining the electric furnace at 150 ° C., 0.5 ⁇ l of pyridine was injected about 4 to 6 times until pulse saturation, and the pyridine was adsorbed to each test example.
- He helium
- the temperature of the electric furnace was increased at a rate of 30 ° C./min, the separated pyridine was measured by FID gas chromatography, and the solid acid amount of each test example was obtained from the peak value of the obtained TPD spectrum.
- FIG. 8 shows the relationship between the amount of solid acid ( ⁇ mol / g ⁇ cat) measured in each of Test Examples 19 to 24 and the SO 3 reduction rate (%).
- the catalyst with a larger amount of solid acid showed a higher SO 3 reduction rate.
- the amount of solid acid was 200 ⁇ mol / g ⁇ cat or more and 300 ⁇ mol / g ⁇ cat or less. From these results, it was found that the higher the amount of solid acid, the more effective the reduction of SO 3 .
- Example 4 Furthermore, a catalyst having another composition was prepared, and the reduction effect of SO 3 to SO 2 by the active metal and the denitration effect were examined.
- Test Example 25 was carried out by adding 80 wt% of water to 20 wt% of catalyst H, performing wet ball milling to obtain a slurry for wash coating, and coating a ceramic substrate containing kaolinite as a main component. Further, a predetermined amount of each sulfate or nitrate solution used as a raw material for V 2 O 5 , MoO 3 , Ag, WO 3 , Mn 2 O 3 , NiO and Co 3 O 4 is added to the catalyst H, After impregnating and supporting, the ceramic substrate was coated in the same manner as in Test Example 25 to obtain Test Examples 26 to 32. The coating amount of each test example was measured in the same manner as in Example 3, and was about 100 g / m 2 . Table 2 shows the composition of each test example.
- FIG. 9 shows the reduction rate (%) and the denitration rate (%) of SO 3 in the combustion exhaust gas with respect to 0.1 m 2 ⁇ h / Nm 3 in Test Examples 24 to 32.
- the SO 3 reduction rate of Test Example 25 was 52.2%.
- SO 3 reduction of the test example 26 is 11.4%
- SO 3 reduction of the test example 27 is 44.5%
- SO 3 reduction of the test Example 28 was 45.8% .
- SO 3 reduction of the test example 29 is 56.0% SO 3 reduction of the test example 30 is 48.3% SO 3 reduction of the test example 31 is 41.8%
- the SO 3 reduction rate of Test Example 32 was 39.7%.
- the denitration rate of Test Example 25 was 60.4%.
- the NOx removal rate of Test Example 26 is 94.4%
- the NOx removal rate of Test Example 27 is 82.4%
- the NOx removal rate of Test Example 28 is 55.5%
- the NOx removal rate of Test Example 29 is The denitration rate in Test Example 30 was 50.9%
- the denitration rate in Test Example 31 was 46.2%
- the denitration rate in Test Example 32 was 44.3%. .
- any test example carrying V 2 O 5 , MoO 3 , Ag, WO 3 , Mn 2 O 3 , MnO 2 , NiO or Co 3 O 4 uses C 3 H 6 as the SO 3 reducing agent.
- SO 3 has a reduction effect and a denitration effect.
- Test Examples 27 to 32 carrying MoO 3 , Ag, WO 3 , Mn 2 O 3 , MnO 2 , NiO or Co 3 O 4 a high SO 3 reduction effect was observed.
- the reduction effect and the denitration effect were recognized especially in Test Example 29 carrying WO 3 . From this, it was found that the catalyst containing WO 3 is effective.
- Example 5 Furthermore, a catalyst having another composition was newly prepared, and both the reducing ability and denitration ability of SO 3 were evaluated.
- Test Example 35 The catalyst J was coated with a metallosilicate at 25 g / m 2 to obtain Test Example 35 using the catalyst K.
- Test Example 36 was carried out using the catalyst B. 100 wt% of the composite oxide per, V 2 O 5 of 0.7 wt%, except that was 9 wt% carrying WO 3, in the same manner as the preparation of the catalyst B, carrying the V 2 O 5 -WO 3 to TiO 2 Prepared Catalyst L was used as Test Example 37. Table 3 shows the composition of each test example.
- FIG. 10 shows the reduction rate (%) of SO 3 in the combustion exhaust gas with respect to 0.1 (1 / AV: m 2 ⁇ h / Nm 3 ) in Test Examples 33 to 37.
- the SO 3 reduction rate of Test Example 33 was 33.3%.
- SO 3 reduction of the test example 34 is 58.4% SO 3 reduction of the test example 35 is 75.6% SO 3 reduction of the test example 36 is 68.6%
- the SO 3 reduction rate of Test Example 37 was 79.9%.
- FIG. 11 shows the denitration rate (%) in the combustion exhaust gas with respect to 0.10 (1 / AV: m 2 ⁇ h / Nm 3 ) in Test Examples 33 to 37.
- the NOx removal rate of Test Example 33 is 95.3%
- the NOx removal rate of Test Example 34 is 95.1%
- the NOx removal rate of Test Example 35 is 91.1%.
- the NOx removal rate of Example 36 was 91.4%
- the NOx removal rate of Test Example 37 was 91.8%.
- Test Examples 34 to 37 showed higher reduction performance of SO 3 to SO 2 as expected than Test Example 33.
- the exhaust gas treatment method and the denitration / SO 3 reduction device According to the exhaust gas treatment method and the denitration / SO 3 reduction device according to the present invention, it is possible to lower the treatment cost than before, denitrate NO X in the combustion exhaust gas, and simultaneously reduce the SO 3 concentration. can do.
- Furnace 2 Flue gas flue 3: ECO 4: ECO bypass 5, 15, 25: Denitration / SO 3 reduction device 6, 16, 26: First injection device 7, 17, 27: Second injection device 8: Catalyst layer 18, 28: First catalyst Layers 19, 29: second catalyst layer
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Abstract
Description
図1は、本発明に係る脱硝・SO3還元装置をボイラの後流に配置した、第一実施の形態を示す。図1に示す脱硝・SO3還元装置5は、火炉1にて燃焼排ガスを発生させるボイラの排ガス煙道2の後流に設けられている。
・チタニア(TiO2)、シリカ(SiO2)、ジルコニア(ZrO2)、酸化セリウム(Ce2O3)の何れか1種の酸化物
・チタン(Ti)、珪素(Si)、ジルコニウム(Zr)又はセリウム(Ce)のうちの2種、3種又は4種の元素からなる混合酸化物若しくは複合酸化物
・2つ、3つ又は4つの前記酸化物からなる混合物
・1つの前記混合物と1つの前記混合物酸化物又は複合酸化物との混合物
これらのうち、前記担体は、TiO2-SiO2、TiO2-ZrO2及びTiO2-CeO2の群より選択された混合酸化物又は複合酸化物が好ましく、前記群より選択された複合酸化物であることがより好ましい。
以上の第一実施の形態に係る脱硝・SO3還元装置の作動形態を説明することにより、本発明に係る排ガス処理方法の第一実施の形態について、説明する。本実施の形態の排ガス処理方法は、SO3還元処理を少なくとも行う。
次に、本発明に係る脱硝・SO3還元装置の第二実施の形態について、図2を参照にして詳細に説明する。なお、本実施の形態では、脱硝・SO3還元装置の第一実施の形態と同じ構成は、同一の符号を付して説明を省略する。本実施の形態に係る脱硝・SO3還元装置15は、触媒層を第一及び第二の触媒層に区分けし、それらの間に第一の注入装置を配置した点で、第一実施の形態の脱硝・SO3還元装置5と相違している。
以上の第二実施の形態に係る脱硝・SO3還元装置の作動形態を説明することにより、本発明に係る排ガス処理方法の第二実施の形態について、説明する。本実施の形態の排ガス処理方法は、SO3還元処理を少なくとも実施する。
次に、本発明に係る脱硝・SO3還元装置の第三実施の形態について、図3を参照にして詳細に説明する。本実施の形態では、脱硝・SO3還元装置の第一及び二実施の形態と同じ構成は、同一の符号を付して説明を省略する。本実施の形態に係る脱硝・SO3還元装置25は、第一の注入装置及び第一の触媒層を、第二の注入装置及び第二の触媒層の前流に配置した点で、第二実施の形態の脱硝・SO3還元装置15と相違している。
続いて、以上の第三実施の形態に係る脱硝・SO3還元装置の作動形態を説明することにより、本発明に係る排ガス処理方法の第三実施の形態について、説明する。本実施の形態の排ガス処理方法は、SO3還元処理を少なくとも実施する。
触媒を変えて、第一の添加剤(SO3還元剤)によるSO3のSO2への還元効果を検討した。
SO3をSO2に還元する触媒としても機能するRu(ルテニウム)を含む触媒Aを調製した。100wt%のチタニア(TiO2)当たり、10wt%の酸化タングステン(WO3)を含有したアナターゼ型チタニア粉末に対して、塩化ルテニウム(RuCl3)水溶液を含浸することにより、100wt%のアナターゼ型チタニア粉末当たり、1wt%のRuを前記粉末に担持させ、蒸発、乾燥した。その後、500℃、5時間焼成を行って、得られた粉末を触媒Aとした。
アンモニアによる脱硝機能を有する代表的な触媒として触媒Bを調製した。TiアルコキシドであるTi(O-iC3H7)4とSiアルコキシドであるSi(OCH3)3とを95:5(それぞれ、TiO2、SiO2として)のwt%比で混合し、80℃の水に添加して加水分解した後、攪拌して熟成させて生成したゾルを濾過し、得られたゲル化物を洗浄、乾燥後、500℃で5時間加熱焼成して、粉末状のTiO2‐SiO2複合酸化物(TiO2‐SiO2粉末)を得た。前記複合酸化物に対して、メタバナジン酸アンモニウム(NH3VO3)とパラタングステン酸アンモニウム((NH4)10H10W12O46・6H2O)を10wt%のメチルアミン水溶液を用いて含浸させ、100wt%の複合酸化物当たり、V2O5を0.6wt%、WO3を8wt%担持させ、蒸発乾固後、500℃で5時間加熱焼成を行なった。得られた粉末を触媒Bとした。
アンモニアによる脱硝機能を有する代表的な触媒Cを調製した。TiアルコキシドであるTi(O-iC3H7)4とZrアルコキシドであるZr(Oi-C4H9)4とを95:5(それぞれ、TiO2、ZrO2として)のwt%比で混合し、80℃の水に添加して加水分解した後、攪拌して熟成させて生成したゾルを濾過し、得られたゲル化物を洗浄、乾燥後、500℃で5時間加熱焼成して、粉末状のTiO2‐ZrO2複合酸化物(TiO2‐ZrO2粉末)を得た。前記複合酸化物に対して、パラタングステン酸アンモニウム((NH4)10H10W12O46・6H2O)を10wt%メチルアミン水溶液で含浸させ、100wt%の複合酸化物当たり、WO3を8wt%担持させ、蒸発乾固後、500℃で5時間加熱焼成を行なった。得られた粉末を触媒Cとした。
チタニア(TiO2)のみの触媒Dを調製した。触媒Aと同量のアナターゼ型チタニア粉末を500℃、5時間焼成を行って、粉末状の触媒Dを調製した。
触媒A~Dの各20wt%に対して、それぞれ水80wt%を加え、湿式ボールミル粉砕を行い、ウォッシュコート用スラリとした。続いて、コージェライト製モノリス基材(7.4mmピッチ、壁厚0.6mm)を上記スラリに浸漬コートし、120℃で乾燥後、500℃で焼成した。コート量は、基材の表面積1m2当たり100gとした。触媒Aを用い、SO3還元剤としてアンモニア(NH3)を用いた場合を試験例1とした。一方、触媒Aを用い、SO3還元剤としてプロピレン(C3H6)を用いた場合を試験例2とした。触媒Bを用い、SO3還元剤としてC3H6を用いた場合を試験例3とした。触媒Cを用い、SO3還元剤としてC3H6を用いた場合を試験例4とした。また、触媒Dを用い、SO3還元剤としてC3H6を用いた場合を試験例5とした。
実機を想定したベンチスケールにて、燃焼排ガスに対して、SO3還元剤を添加し、脱硝・SO3還元装置内に設置した各試験例の触媒層を通過させることにより、触媒層通過前後の0.03~0.08(1/AV(m2・h/Nm3))に対する燃焼排ガス中のSO3濃度(ppm)の変化を検討した。試験結果及び試験条件を図4に示す。なお、SO3濃度は、サンプリング後、沈殿滴定法により分析した。また、図中、AVは面積速度(ガス量/触媒での全接触面積)を示し、1/AVはガス量に対する触媒の全接触面積を意味する。1/AVの単位は、m2・h/Nm3と示される。
1.炭化水素の吸着反応
炭化水素(CxHy)+表面→CxHy-表面
2.炭化水素の分解反応(水素引き抜き)
CxHy-表面→CxHy-1(表面配位)+H-表面
3.SO3(g)との反応(スルホン酸化)
CxHy-1(表面配位)+SO3(g)→SO2+CxHy-1-SO3--H-
表面
4.SO3分解
CxHy-1-SO3--H-表面→SO2+CO2+CO
組成の異なる炭化水素を第一の添加剤(SO3還元剤)として用い、炭化水素化合物の組成によるSO3のSO2への還元効果を検討した。
触媒Bを、実施例1と同様にして、コージェライト製モノリス基材上にコートした。コート量は、基材の表面積1m2当たり100gとした。SO3還元剤としてC3H6を用いた場合を試験例6とし、プロパン(C3H8)を用いた場合を試験例7とし、メタノール(CH3OH)を用いた場合を試験例8とし、エタノール(C2H5OH)を用いた場合を試験例9とした。また、他の試験例と比較するために、SO3還元剤としてアンモニア(NH3)を用いた場合を試験例10とした。
実施例1と同様に、燃焼排ガスに対して、SO3還元剤を添加し、前期脱硝・SO3還元装置内に設置したSO3触媒を用いた触媒層を通過させることにより、触媒層通過前後の0.04~0.08m2・h/Nm3に対する燃焼排ガス中のSO3濃度の変化を検討した。触媒層通過前後のSO3濃度の変化を検討した。なお、試験条件は、実施例1と同条件とした。試験結果及び試験条件を図5に示す。
TiO2、SiO2としてのwt%比を88:12とし、100wt%の複合酸化物当たり、V2O5を0.3wt%、WO3を9wt%としたこと以外、触媒Bと同様にして、触媒Eを調製した。
触媒Eを、実施例1と同様に、コージェライト製モノリス基材上にコートした。これに、SO3還元剤としてメタノール(CH3OH)を用いた場合を試験例11とし、エタノール(C2H5OH)を用いた場合を試験例12とし、プロパン(C3H8)を用いた場合を試験例13とした。また、SO3還元剤としてエチレン(C2H4)を用いた場合を試験例14とし、プロピレン(C3H6)を用いた場合を試験例15とし、1-ブテン(1-C4H8)を用いた場合を実施例16とし、2-ブテン(2-C4H8)を用いた場合を試験例17とし、イソブテン(iso-C4H8)を用いた場合を試験例18とした。
試験例11~18を用いて、実施例1と同様に、燃焼排ガスに対してSO3還元剤を添加し、脱硝・SO3還元装置内に設置したSO3触媒を用いた触媒層を通過させることにより、触媒層通過前後のSO3濃度及び脱硝率の変化を検討した。なお、SO3還元率及び脱硝率は以下のようにして求めた。試験結果及び試験条件を図6に示す。
SO3還元率(%)=(1-触媒層出口SO3濃度/触媒層入口SO3濃度)×100
脱硝率(%)=(1-触媒層出口NOX濃度/触媒層入口NOX濃度)×100
さらに別の組成の触媒を調製し、触媒組成によるSO3のSO2への還元効果及び脱硝効果を検討した。
TiアルコキシドであるTi(O-iC3H7)4とCeアルコキシドであるCe(OCH3)4とを、88:12(それぞれ、TiO2、Ce2O3として)のwt%比で混合し、80℃の水に添加して加水分解した後、攪拌して熟成させて生成したゾルを濾過し、得られたゲル化物を洗浄、乾燥後、500℃で5時間加熱焼成して、TiO2‐Ce2O3複合酸化物(TiO2‐Ce2O3粉末)を得た。得られた粉末を触媒Fとした。
ジルコニア(ZrO2)のみの触媒を調製した。オキシ塩化ジルコニウム(ZrOCl2)粉末を500℃、5時間で焼成し、得られた粉末を触媒Gとした。
酸化セリウム(Ce2O3)のみの触媒を調製した。硝酸セリウム(Ce(NO3)2)粉末を500℃、5時間で焼成し、得られた粉末を触媒Hとした。
触媒D、BのTiO2‐SiO2粉末、CのTiO2‐ZrO2粉末、F、G及びHの各20wt%に対して、それぞれ、水80wt%を加え、湿式ボールミル粉砕を行い、ウォッシュコート用スラリとした後、カオリナイトを主成分としたセラミクス基材にコートし、試験例19~24とした。各試験例の組成を表1に示す。なお、表中、コート量平均値は、コート前後の重量差より得られた担持量を基材表面積で除した値を用いて2サンプル測定した平均値を用いた。
各試験例に対して、SO3還元剤としてプロピレン(C3H6)を用いた場合のSO3の還元能力を検討した。実施例2と同様にして、燃焼排ガスに対して、SO3還元剤を添加し、脱硝・SO3還元装置内に設置したSO3触媒を用いた触媒層を通過させることにより、触媒層通過前後のSO3濃度の変化を検討した。試験結果及び試験条件を図7に示す。
続いて、固体酸量とSO3還元率との関連性を検討した。試験例19~24の固体酸量は、ピリジン昇温吸着離脱法により測定した。より具体的には、各試験例25mgの同量の石英粉末を加えて、石英ガラス管にカオウールで固定した。石英ガラス管をFIDガスクロマトグラフィーに設けられた電気炉に設置した後、ヘリウム(He)気流中にて温度450℃、30分の条件下で処理した。その後、電気炉を150℃に保ちピリジンを0.5μlずつ、パルス的に飽和になるまで4回~6回程度注入し、前記ピリジンを各試験例に吸着させた。続いて、電気炉を30℃/分の速度で昇温し、離脱したピリジンをFIDガスクロマトグラフィーで測定し、得られたTPDスペクトルのピーク値から各試験例の固体酸量を求めた。
さらに別の組成の触媒を調製し、活性金属によるSO3のSO2への還元効果と脱硝効果とを検討した。
TiアルコキシドであるTi(O-iC3H7)4とSiアルコキシドであるSi(OCH3)3とを95:5(それぞれ、TiO2、SiO2として)のwt%比で混合し、80℃の水に添加して加水分解した後、攪拌して熟成させて生成したゾルを濾過し、得られたゲル化物を洗浄、乾燥後、500℃で5時間加熱焼成して、TiO2‐SiO2複合酸化物(TiO2‐SiO2粉末)を得た。得られた粉末を触媒Hとした。
20wt%の触媒Hに対して、水80wt%を加え、湿式ボールミル粉砕を行い、ウォッシュコート用スラリとした後、カオリナイトを主成分としたセラミクス基材にコートして、試験例25とした。また、触媒Hに、それぞれ、V2O5、MoO3、Ag、WO3、Mn2O3、NiO及びCo3O4の原料として用いた各硫酸塩もしくは硝酸塩溶液を所定量添加して、含浸担持させた後、試験例25と同様にしてセラミクス基材にコートし、試験例26~32とした。各試験例のコート量は、実施例3と同様にして測定し、100g/m2程度とした。各試験例の組成を表2に示す。
各試験例に、SO3還元剤として、プロピレン(C3H6)を用いた場合のSO3の還元能力を検討した。実施例2と同様にして、燃焼排ガスに対してSO3還元剤を添加し、脱硝・SO3還元装置内に設置したSO3触媒を用いた触媒層を通過させることにより、触媒層通過前後のSO3濃度の変化を検討した。試験結果及び試験条件を図9に示す。
さらに別の組成の触媒を新たに準備し、SO3の還元能力と脱硝能力との両方を評価した。
100wt%の複合酸化物当たり、メタバナジン酸アンモニウムを用いてV2O5を0.3wt%、パラタングステン酸アンモニウムを用いてWO3を9wt%を溶液にして同時担持させたこと以外、触媒Bの調製と同様にして、TiO2にV2O5‐WO3を担持させた触媒Iを準備し、試験例33とした。100wt%の複合酸化物当たり、V2O5を0.3wt%、WO3を9wt%担持させたこと以外、触媒Bの調製と同様に、TiO2‐SiO2複合酸化物にV2O5‐WO3を担持させた触媒Jを、試験例34とした。触媒Jに25g/m2でメタロシリケートをコートして触媒Kを用いた試験例35とした。触媒Bを用いて試験例36とした。100wt%の複合酸化物当たり、V2O5を0.7wt%、WO3を9wt%担持させたこと以外、触媒Bの調製と同様にして、TiO2にV2O5‐WO3を担持させた触媒Lを準備し、試験例37とした。各試験例の組成を表3に示す。
各試験例に、SO3還元剤として、プロピレン(C3H6)を用いた場合のSO3の還元能力を検討した。実施例2と同様にして、燃焼排ガスに対して、SO3還元剤を添加し、脱硝・SO3還元装置内に設置したSO3触媒を用いた触媒層を通過させることにより、触媒層通過前後のSO3濃度の変化と脱硝率を検討した。試験結果及び試験条件を図10及び図11に示す。
2:排ガス煙道
3:ECO
4:ECOバイパス
5、15、25:脱硝・SO3還元装置
6、16、26:第一の注入装置
7、17、27:第二の注入装置
8:触媒層
18、28:第一の触媒層
19、29:第二の触媒層
Claims (14)
- NOXに加え、SO3を含有する燃焼排ガスに、第一の添加剤として炭素数3~5のオレフィン系炭化水素(不飽和炭化水素)を添加した後、Ti、Si、Zr及びCeからなる群より選ばれる元素の1種以上の酸化物及び/又は前記群より選ばれる元素の2種以上の混合酸化物及び/又は複合酸化物を担体として含み、貴金属を含まない触媒に接触させSO3をSO2に還元処理することを特徴とする排ガス処理方法。
- 前記炭素数3~5のオレフィン系炭化水素(不飽和炭化水素)が、C3H6、C4H8及びC5H10からなる群より選ばれる1種以上のものである請求項1に記載の排ガス処理方法。
- 前記C4H8及びC5H10が、何れか一の幾何異性体又はラセミ体である請求項2に記載の排ガス処理方法。
- 前記担体が、TiO2-SiO2、TiO2-ZrO2及びTiO2-CeO2からなる群より選択された1種以上の混合酸化物及び/又は複合酸化物からなる請求項1~3の何れか一項に記載の排ガス処理方法。
- 前記触媒が、前記複合酸化物を担体として、V2O5、WO3、MoO3、Mn2O3、MnO2、NiO及びCo3O4からなる群より選択される1種以上の金属酸化物を担持してなる触媒である請求項1~4の何れか一項に記載の排ガス処理方法。
- 前記触媒に、ゼオライト結晶構造中のAl及び/又はSiの少なくとも一部を、Ti、V、Mn、Fe及びCоからなる群より選ばれる1種以上で置換したメタロシリケート系複合酸化物をコートした請求項5に記載の排ガス処理方法。
- 前記SO3をSO2に還元する処理が、250℃以上450℃以下の温度範囲内で行われる請求項1~6の何れか一項に記載の排ガス処理方法。
- 前記SO3をSO2に還元する処理が、300℃以上400℃以下の温度範囲内で行われる請求項7に記載の排ガス処理方法。
- NOXに加え、SO3を含有する燃焼排ガスに第一の添加剤を添加する第一の注入装置と、
前記燃焼排ガスが通過する触媒からなる触媒層と
を備え、
第一の添加剤が炭素数3~5のオレフィン系炭化水素(不飽和炭化水素)であり、前記触媒が、貴金属を含まず、且つTi、Si、Zr及びCeからなる群より選ばれる元素の1種以上の酸化物及び/又は前記群より選ばれる元素の2種以上の混合酸化物及び/又は複合酸化物を担体としてなり、SO3をSO2に還元処理することを特徴とするSO3還元装置。 - 前記炭素数3~5のオレフィン系炭化水素(不飽和炭化水素)が、C3H6、C4H8及びC5H10からなる群より選ばれる1種以上のものである請求項9に記載のSO3還元装置。
- 前記C4H8及びC5H10が、何れか一の幾何異性体又はラセミ体である請求項10に記載のSO3還元装置。
- 前記担体が、TiO2-SiO2、TiO2-ZrO2及びTiO2-CeO2からなる群より選択された1種以上の混合酸化物及び/又は複合酸化物からなる請求項9~11の何れか一項に記載のSO3還元装置。
- 前記触媒が、前記複合酸化物を担体として、V2O5、WO3、MoO3、Mn2O3、MnO2、NiO及びCo3O4からなる群より選択される1種以上の金属酸化物を担持してなる触媒である請求項9~12の何れか一項に記載のSO3還元装置。
- 前記触媒層が、前記第一の注入装置の後流に配置されたSO3濃度を低減させる第一の触媒層と、前記第一の注入装置に近設されて、前記燃焼排ガスに第二の添加剤としてNH3を添加する第二の注入装置の後流に配置された脱硝を行う第二の触媒層とからなり、
前記第一の触媒層を前記第二の触媒層の前流又は後流に配置した請求項9~13の何れか一項に記載のSO3還元装置。
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