Patent Application
20190232221
The present invention relates to an exhaust gas treatment catalyst, a method for producing an exhaust gas treatment catalyst, and an exhaust gas treatment system and particularly to an exhaust gas treatment catalyst that uses carbon monoxide (CO) in an exhaust gas generated in a sintering furnace as a reducing agent or a fuel for heating, a method for producing an exhaust gas treatment catalyst, and an exhaust gas treatment system. Priority is claimed on the basis of Japanese Patent Application No. 2016-150470, filed on Jul. 29, 2016, the content of which is incorporated herein by reference.
In the related art, as a method for treating an exhaust gas generated from a sintering furnace in an iron-making plant or the like, a technique of reducing and denitrating nitrogen monoxide (NO) on a denitration catalyst using ammonia (NH3) as a reducing agent is known. In addition, in the case of denitration using ammonia as a reducing agent, it is necessary to separately use a facility for adding ammonia or a fuel for heating for increasing a reaction temperature of the denitration. Therefore, a denitration method in which Co is used as a reducing agent and a fuel for heating has been used. In addition, a method for reducing the fuel for heating using an amount of heat generated by oxidation of CO also has been used.
As a catalyst that is used in the above-described denitration method, a catalyst in which iridium (Ir), potassium (K), and tin (Sn) are dispersed in and supported by a carrier having a low specific surface area which is made of silicon carbide (SiC) and a crystallite diameter of iridium is set in a range of 2 to 100 nm is known (for example, PTL 1). In addition, as a catalyst using an amount of heat generated by oxidation of CO, a catalyst in which platinum (Pt) is supported by a carrier that is a monoxide of one or more selected from the group consisting of titanium dioxide (TiO2) and zirconium dioxide (ZrO2) or a complex oxide thereof is known (for example, PTL 2).
[PTL 1] Japanese Unexamined Patent Application Publication No. 8-309186
[PTL 2] Japanese Unexamined Patent Application Publication No. 2005-270821
However, in the above-described examples, in the case of denitrating an exhaust gas using CO as a reducing agent, there is a problem in that a CO denitration reaction that converts NO to nitrogen (N2) using CO and a CO oxidation reaction in which CO is oxidized to CO2 selectively progress as described in Expressions (i) and (ii) and thus a desired NO conversion rate cannot be obtained. In addition, in the case of oxidizing CO in an exhaust gas using a catalyst, there is a problem in that a desired CO oxidation rate cannot be obtained.
2CO+2NO→N2+2CO2 (i)
2CO+O2→2CO2 (ii)
In consideration of the above-described circumstance, an object of the present invention is to provide an exhaust gas treatment catalyst capable of improving a NO conversion rate in denitration using CO as a reducing agent and capable of improving a CO oxidation rate in an oxidation of CO in an exhaust gas, a method for producing an exhaust gas treatment catalyst, and an exhaust gas treatment system.
As a result of creative studies, the present inventors found that, when a specific surface area of an exhaust gas treatment catalyst that has been produced as a catalyst by supporting iridium by a carrier that is a metal oxide or a metal sulfoxide and a crystallite diameter of iridium in the catalyst are set to predetermined values, it is possible to improve performance of the catalyst such as a NO conversion rate and a CO oxidation rate and completed the present invention.
At least an aspect of the present invention is an exhaust gas treatment catalyst. An exhaust gas treatment catalyst according to the present invention is a catalyst for treating an exhaust gas from a sintering furnace using CO as a reducing agent, the exhaust gas treatment catalyst including: a carrier that is a metal oxide or a metal sulfoxide and an active metal including at least iridium supported by the carrier, in which a specific surface area of the catalyst is 100 m2/g or less, and a crystallite diameter of iridium in the catalyst is 10 nm or more and 25 nm or less.
In addition, the crystallite diameter of iridium in the catalyst is preferably 10 nm or more and 23 nm or less.
Another aspect of the present invention is a method for producing an exhaust gas treatment catalyst. A method for producing an exhaust gas treatment catalyst according to the present invention is a method for producing the exhaust gas treatment catalyst, including: an impregnation and supporting step of impregnating the carrier with iridium to be supported thereby, a firing step of firing the carrier supporting iridium, and an activation step of activating the carrier by heating the carrier in a reducing gas atmosphere after the firing, in which a specific surface area of the carrier in the impregnation and supporting step is 100 m2/g or less.
Still another aspect of the present invention is an exhaust gas treatment system. An exhaust gas treatment system of the present invention is an exhaust gas treatment system for denitrating an exhaust gas from a sintering furnace using CO as a reducing agent, the exhaust gas treatment system including: a denitration device including the exhaust gas treatment catalyst, a heating device that is provided upstream of the denitration device and heats the exhaust gas up to a predetermined temperature at the time of start-up, and a heating and heat recovery device that is provided upstream and downstream of the denitration device and the heating device, heats the exhaust gas using a medium, and recovers heat of the exhaust gas flowing therein from the denitration device using the medium. Meanwhile, as the heating device, a duct burner is assumed, and a fuel is cokes oven gas (COG) emitted from the same iron-making plant.
Furthermore, far still another aspect of the present invention is an exhaust gas treatment system. The system is an exhaust gas treatment system for using an amount of heat generated from oxidation of CO as a heat source of a denitration device, the exhaust gas treatment system including: a denitration device including a denitration catalyst, a heating device that is provided upstream of the denitration device and heats the exhaust gas up to a predetermined temperature at the time of start-up, the exhaust gas treatment catalyst provided downstream of the denitration device, and a heating and heat recovery device that is provided upstream and downstream of the denitration device and the heating device, heats the exhaust gas using a medium, and recovers heat of the exhaust gas flowing therein from the denitration device using the medium.
According to the present invention, an exhaust gas treatment catalyst capable of improving a NO conversion rate in denitration using CO as a reducing agent and capable of improving a CO oxidation rate in the oxidation of CO in an exhaust gas, a method for producing an exhaust gas treatment catalyst, and an exhaust gas treatment system are provided.
Hereinafter, an embodiment of an exhaust gas treatment catalyst, a method for producing an exhaust gas treatment catalyst, and an exhaust gas treatment system according to the present invention will be described in detail with reference to drawings. Meanwhile, the present invention is not limited to the embodiment described below.
A first embodiment of the exhaust gas treatment catalyst according to the present invention will be described. The exhaust gas treatment catalyst according to the present embodiment is a denitration catalyst for using CO in an exhaust gas generated by combustion in a sintering furnace of an iron-making plant (hereinafter, also referred to as the sintering furnace exhaust gas) as a reducing agent and a fuel for heating and includes a carrier and iridium (Ir) as an active metal.
In the sintering furnace exhaust gas that is a treatment subject of the exhaust gas treatment catalyst, CO that is a reducing gas is included in a high concentration of 4,000 to 20,000 ppm. Therefore, CO in the sintering furnace exhaust gas is used as a reducing agent of a denitration reaction, and CO that does not contribute to the denitration reaction is oxidized and combusted. Therefore, a denitration method in which CO is used to heat the sintering furnace exhaust gas becomes possible, and it is possible to significantly reduce a reducing agent and a fuel cost. The concentration of CO in the sintering furnace exhaust gas is preferably 6,000 ppm or more. When the concentration is 6,000 ppm or more, it is possible to improve the NO conversion rate by efficiently using CO in the sintering furnace exhaust gas.
The carrier in the exhaust gas treatment catalyst needs to be a carrier raw material that is capable of supporting metallic iridium as an active metal and has a specific surface area of 100 m2/g or less. Examples of the carrier raw material include a metal oxide or a metal sulfoxide. The metal oxide is preferably an oxide or a complex oxide of one or more metals selected from the group consisting of titanium (Ti), silicon (Si), aluminum (Al), zirconium (Zr), and cerium (Ce) and more preferably titanium dioxide (TiO2) or silicon dioxide (SiO2). The metal sulfoxide is preferably barium sulfate (BaSO4), calcium sulfate (CaSO4), or strontium sulfate (SrSO4).
The specific surface area of the exhaust gas treatment catalyst needs to be an area in which the metallic iridium can be supported. More specifically, a lower limit value of the specific surface area of the exhaust gas treatment catalyst is preferably set to 0.5 m2/g or more and is preferably 12 m2/g or more. When the specific surface area of the exhaust gas treatment catalyst is less than 0.5 m2/g, there is a concern that denitration performance may significantly degrade. In addition, an upper limit value of the specific surface area of the exhaust gas treatment catalyst can be set to 100 m2/g or less and is preferably 90 m2/g or less and more preferably 20 m2/g or less. The specific surface area of the exhaust gas treatment catalyst is, for example, a BET specific surface area calculated using a BET method.
A lower limit value of a crystallite diameter of the metallic iridium in the exhaust gas treatment catalyst is preferably 10 nm or more. In addition, an upper limit value of the crystallite diameter of the metallic iridium in the catalyst is preferably 30 nm or less, more preferably 25 nm or less, and still more preferably 23 nm or less. In addition, the crystallite diameter of the metallic iridium in the catalyst is particularly preferably 12 nm or more and 23 nm or less. When the crystallite diameter of the metallic iridium exceeds 30 nm, there is a concern that a reactivity of the denitration reaction may degrade. An amount of the metallic iridium supported by the carrier needs to be an amount at which the crystallite diameter of the metallic iridium is in the above-described range and can be set to, for example 0.25% to 2% by weight of the carrier.
As described above, when the specific surface area of the exhaust gas treatment catalyst is set in a predetermined range, and the crystallite diameter of the metallic iridium in the exhaust gas treatment catalyst is set in a predetermined range, it is possible to achieve a NO conversion rate of 60% or more in denitration using CO as a reducing agent.
An embodiment of a method for producing the exhaust gas treatment catalyst having the above-described constitution will be described.
First, in the impregnation and supporting step, an iridium aqueous solution containing at least an iridium element is impregnated into a carrier having a predetermined specific surface area, thereby impregnating a surface of the carrier (S1) with an iridium compound to be supported thereby. The specific surface area of the carrier is, for example, a BET specific surface area calculated using a BET method.
In the impregnation and supporting step, an upper limit value of the specific surface area of the carrier needs to be in a range in which the carrier can be impregnated with iridium and is capable of supporting iridium and is preferably 100 m2/g or less, more preferably 80 m2/g or less, and still more preferably 22 m2/g or less. In addition, a lower limit value of the specific surface area of the carrier needs to be in a range in which the carrier can be impregnated with iridium and is capable of supporting iridium and is preferably 0.5 m2/g or more, more preferably 12 m2/g or more, and still more preferably 14 m2/g or more. When the specific surface area of the carrier is less than 0.5 m2/g, there is a concern that the denitration performance may significantly degrade. When the specific surface area of the carrier is in the above-described range, it is possible to preferably grow the crystallite diameter of iridium and improve the NO conversion rate in denitration using CO as a reducing agent.
Next, the carrier is treated at a predetermined temperature for a predetermined time, thereby evaporating moisture in the carrier and drying the carrier (S2). The dried carrier is dried in the air at a predetermined temperature for a predetermined time (S3), thereby obtaining a catalyst supporting the iridium compound. The temperature and the time during the evaporation and drying the carrier need to be a temperature and a time at which the carrier can be dried and can be set to, for example, a temperature of 140° C. and three hours. In addition, the temperature and the time during the drying of the dried catalyst need to be a temperature and a time at which the carrier can be sufficiently dried and can be set to, for example, a temperature of 110° C. and 12 hours.
The iridium aqueous solution that is used in the impregnation and supporting step needs to be an aqueous solution in which iridium can be impregnated into and supported by the carrier by means of immersion, and examples thereof include an iridium (III) chloride solution (H3IrCl6), an iridium (II) chloride solution (H2IrCl6), a sodium hexachloride iridate (III) solution (Na3IrCl6), a sodium hexachloride iridate (II) solution (Na2IrCl6), a sodium hexabromo iridate (III) solution (Na2IrBr6), a haxaammineiridium (III) chloride solution (Ir(NH3)6Cl3), a haxaammineiridium (III) hydroxide solution (Ir(NH3)6(OH)3), a haxaammineiridium (III) nitrate solution (Ir(NH3)6(NO3)3), and the like. Among these, practically, an iridium (II) chloride solution is preferred.
As the carrier in the catalyst that is used in the impregnation and supporting step, it is possible to preferably employ the above-described carrier in the denitration catalyst according to the present embodiment.
In the first firing step, the dried carrier is heated to a predetermined temperature for a predetermined time, whereby an iridium salt on the surface of the carrier is decomposed and oxidized, and a powder-form catalyst in which iridium oxide is supported as an active metal is obtained (S4).
A firing temperature in the first firing step can be set to, for example, 400° C. or higher and 1,000° C. or lower and is preferably 500° C. or higher and 800° C. or lower. In addition, a firing time in the firing step is preferably set to three hours or longer and eight hours or shorter. In addition, a temperature-increase rate in the first firing step also varies depending on the firing time and the firing temperature, but can be set to, for example, 100° C./h. When the temperature, the time, and the temperature-increase rate in the first firing step are in the above-described ranges, it is possible to preferably grow the crystallite diameter of iridium in the denitration catalyst and improve the NO conversion rate in denitration using CO as a reducing agent.
Next, water (H2O) is added to the powder-form catalyst in a wet-type ball mill container, and the catalyst is crushed under predetermined conditions, thereby obtaining a slurry for wash coating (S5). The crushing conditions with a wet-type ball mill can be set to, for example, room temperature, eight hours, and a rotation speed of 100 rpm.
Next, the slurry is moved to another container provided with a stirrer, a honeycomb-shaped monolith base material is immersed in the slurry to carry out wash coating, a surplus slurry is blown away as necessary, and the monolith base material is dried at a predetermined temperature for a predetermined time (S6). Examples of the monolith base material include ceramic monolith base materials such as cordierite, titanium oxide monolith base materials, and the like. A coating amount can be set to, for example, 100 g/m2 or less. A drying temperature and a time in the drying step need to be a temperature and a time at which the carrier can be sufficiently dried and can be set to, for example, a temperature of 120° C. for two hours.
In the second firing step, the honeycomb-shaped catalyst is heated and fired at a predetermined temperature for a predetermined time (S7). A firing temperature in the second firing step can be set to, for example, 400° C. or higher and 1,000° C. or lower and is preferably 500° C. or higher and 800° C. or lower. A firing time in the firing step is preferably three hours or longer and eight hours or shorter. In addition, a temperature-increase rate in the second firing step also varies depending on the firing time and the firing temperature, but can be set to, for example, 100° C./h.
In the activation step, the catalyst supporting iridium is heated at a predetermined temperature for a predetermined time using a reducing gas, whereby iridium oxide in the catalyst is reduced to produce metallic iridium, and a catalyst in which the crystallite diameter of iridium is set in a predetermined range is obtained (S8).
A temperature in the activation step can be set to, for example, 400° C. or higher and 1,000° C. or lower and is preferably 500° C. or higher and 800° C. or lower. In addition, a time in the activation step can be set to, for example, 0.5 hours or longer and 50 hours or shorter. When the temperature and/or the time in the activation step are in the above-described ranges, it is possible to preferably grow the crystallite of iridium in the denitration catalyst and improve the NO conversion rate in denitration using CO as a reducing agent.
Examples of the reducing gas that is used in the activation step include gases such as hydrogen (H2), carbon monoxide (CO), gas mixtures thereof, and hydrocarbons. Among these, from the viewpoint of an intensity of a reducing property, the reducing gas is preferably hydrogen, carbon monoxide, or a gas mixture thereof. Regarding a concentration of the reducing gas in the activation step, for example, in a case in which hydrogen is used as the reducing gas, the concentration of the reducing gas is 4% by volume or less, and, in a case in which hydrogen monoxide is used as the reducing gas, the concentration of the reducing gas is 12.5% by volume or less. In addition, in a case in which a gas mixture of hydrogen and carbon monoxide is used as the reducing gas, the concentration thereof is equal to or less than a concentration obtained by further industrially applying a safety rate according to the Le Chatelier's principle depending on a mixing proportion. For example, as shown in the following expression, an upper limit value of a concentration L (% by volume) of a gas mixture is calculated from values of a percent by volume of hydrogen (n), a percent by volume of carbon monoxide (m) and the safety rate k (0.2 to 0.8). In addition, components other than what has been described above in the reducing gas, an inert component such as nitrogen (N2) or argon (Ar) is exemplified.
The crystallite diameter of iridium can be measured using an X-ray diffraction method, an XPS method, an EXAFS method, a TEM method, or the like. For example, the crystallite diameter of iridium can be calculated from a full width at half maximum of a diffraction peak obtained using an X-ray diffraction method using the Sherrer equation.
An embodiment of an exhaust gas treatment system to which the exhaust gas treatment catalyst produced using the above-described production method is applied will be described using
As illustrated in
The heating and heat recovery device 10 is a gas gas heater (GGH) provided upstream of the heating device 20 and downstream of the denitration device 30 along the flow of an exhaust gas. The heating and heat recovery device 10 is constituted so as to include at least one heat exchanger and a heat medium that circulates in the heating and heat recovery device, to heat an exhaust gas from a sintering furnace through heat exchange with the heat medium such as water, and to recover heat from an exhaust gas that has passed through the denitration device 30 using the heat medium. In addition, the heating and heat recovery device 10 is constituted so as to send an exhaust gas from which heat has been recovered downstream of a chimney or the like.
Upstream of the heating and heat recovery device 10, a dust precipitator and/or a desulfurization device, not illustrated, can be provided. The dust precipitator is an electrostatic precipitator (EP) or a bag filter installed in an existing plant. The dust precipitator is constituted so as to trap soot and dust in an exhaust gas using the electrostatic precipitator (EP) or the bag filter. In addition, the desulfurization device is a flue-gas desulfurization (FGD) that is, preferably, provided downstream of the dust precipitator and installed in an existing plant. A smoke exhaust and desulfurization device is a dry-type or wet-type desulfurization device. In the case of a dry-type desulfurization device, the desulfurization device is constituted so as to spray hydrated lime (Ca(OH)2) or soda (NaHCO3) as a desulfurization agent to the exhaust gas before trapping by the bag filter and absorb SO2 in a surface deposition layer of the bag filter, thereby carrying out desulfurization. In the case of the wet-type desulfurization device, the desulfurization device is constituted so as to bring residual or reduced SO2 in an exhaust gas into contact with a lime slurry formed by suspending lime stone (CaCO3) in water, thereby absorbing and removing SO2. In addition, the desulfurization device is constituted so as to oxidize the lime slurry that has absorbed SO2 using the air supplied from an air supply line, not illustrated, to produce a gypsum slurry (CaSO4.2H2O) and trap and remove SO2 in a gypsum form. A temperature of the exhaust gas that has passed through the dust precipitator and/or the desulfurization device is, for example, approximately 160° C. upstream of the heating and heat recovery device 10.
The heating device 20 is, for example, a duct burner provided downstream of the heating and heat recovery device 10 and upstream of the denitration device 30. The heating device 20 is constituted so as to heat an exhaust gas using cokes oven gas (COG) emitted from the same iron-making plant as a fuel and CO in the exhaust gas as a fuel for heating and a reducing agent up to 200° C. to 270° C. at which the exhaust gas can be preferably denitrated and send the exhaust gas to the denitration device 30.
The denitration device 30 is provided downstream of the heating device 20 and upstream of the heating and heat recovery device 10. The denitration device 30 is a fixed bed-type, movable bed-type, or fluidized bed-type denitration device. The denitration device 30 is constituted so as to include the catalyst described in the present specification therein and denitrate an exhaust gas using CO in the exhaust gas as a reducing agent.
According to the exhaust gas treatment catalyst, the method for producing an exhaust gas treatment catalyst, and the exhaust gas treatment system according to the present embodiment, it is possible to accelerate a CO denitration reaction and improve the NO conversion rate in a denitration treatment of an exhaust gas using an exhaust gas treatment catalyst as a denitration catalyst.
A second embodiment of the exhaust gas treatment catalyst according to the present invention will be described. The exhaust gas treatment catalyst according to the present embodiment is a catalyst for oxidizing CO in an exhaust gas generated by combustion in a sintering furnace of an iron-making plant and using an amount of heat generated as a heat source for denitration (hereinafter, also referred to as the CO oxidation catalyst). The CO oxidation catalyst according to the present embodiment is different from the first embodiment mainly in a range of a crystallite diameter of metallic iridium.
A lower limit value of a crystallite diameter of the metallic iridium in the exhaust gas treatment denitration catalyst is preferably 10 nm or more. In addition, an upper limit value of the crystallite diameter of the metallic iridium in the catalyst is preferably 23 nm or less. In addition, the crystallite diameter of the metallic iridium in the catalyst is particularly preferably 12 nm or more and 23 nm or less. When the crystallite diameter of the metallic iridium exceeds 23 nm, there is a concern that a reactivity of a reaction may degrade. An amount of the metallic iridium supported by the carrier needs to be an amount at which the crystallite diameter of the metallic iridium is in the above-described range and can be set to, for example 0.25% to 2% by weight of the carrier.
As described above, when a specific surface area of the exhaust gas treatment catalyst is set in a predetermined range, and the crystallite diameter of the metallic iridium in the exhaust gas treatment catalyst is set in a predetermined range, it is possible to achieve a CO oxidation rate of 80% or more in the oxidation of CO in the exhaust gas.
An embodiment of a method for producing the exhaust gas treatment catalyst having the above-described constitution will be described. The method for producing an exhaust gas treatment catalyst according to the present embodiment is different from the first embodiment mainly in a temperature condition in an activation step. A temperature in the activation step can be set to, for example, 400° C. or higher and 1,000° C. or lower and is preferably 500° C. or higher and 600° C. or lower. In addition, a time in the activation step can be set to, for example, 0.5 hours or longer and 50 hours or shorter. When the temperature and/or the time in the activation step are in the above-described ranges, it is possible to preferably grow iridium crystallites in the denitration catalyst and improve the CO oxidation rate in the oxidation of CO in the exhaust gas.
A second embodiment of an exhaust gas treatment system to which the exhaust gas treatment catalyst produced using the above-described production method is applied will be described using
The CO oxidation catalyst portion is constituted so as to include the exhaust gas treatment catalyst of the second embodiment therein, to be located downstream of the denitration device 30, and to oxidize CO in the exhaust gas.
According to the exhaust gas treatment catalyst, the method for producing an exhaust gas treatment catalyst, and the exhaust gas treatment system according to the present embodiment, it is possible to accelerate a CO oxidation reaction and improve the CO oxidation rate in the oxidation of CO in an exhaust gas using an exhaust gas treatment catalyst as a CO oxidation catalyst.
Hereinafter, the present invention will be more specifically described using test examples and comparative examples. The exhaust gas treatment catalyst, the method for producing an exhaust gas treatment catalyst, and the exhaust gas treatment system according to the present invention are not limited by the following description.
In Test Example 1, silicon dioxide (SiO2) having a specific surface area of 80 m2/g was used as a carrier in a catalyst. In an impregnation and supporting step, this carrier (99.5 g) was impregnated with an iridium (II) chloride solution (5.8 g) having a concentration of 8.6×10−2% by weight, evaporated and solidified at 140° C. for three hours, and then dried for one night at 110° C. in the air.
Next, as a first firing step, the dried catalyst was fired in a firing furnace at 800° C. for five hours, thereby obtaining a powder. Water (80% by mass) was added to the obtained powder (20% by mass), and the powder was crushed in a wet-type ball mill at 100 rpm for eight hours, thereby preparing a slurry for wash coating. A titanium oxide (TiO2) honeycomb-shaped monolith base material (7.4 mm pitch, wall thickness: 1.15 mm) was immersed in this slurry to carry out wet coating and was dried at 120° C. A coating amount was set to 100 g per square meter of a surface area of the base material.
Next, as a second firing step, the dried catalyst was fired in a firing furnace at 500° C. for five hours.
Next, as an activation step, the fired catalyst was activated by reducing iridium oxide at 600° C. for one hour using hydrogen (H2) having a concentration of 3% by volume as a reducing gas. The activated catalyst was used as an exhaust gas treatment catalyst of Test Example 1.
In Comparative Example 1, a catalyst prepared in the same manner as in Test Example 1 except for the fact that silicon dioxide having a specific surface area of 300 m2/g was used as the carrier was used.
Denitration performance and CO oxidation performance of Test Example 1 and Comparative Example 1 were measured in a laboratory scale. First, the denitration performance and the CO oxidation performance of the test example and the comparative example were measured using a tube-type communication reaction tester and gases having properties shown in Table 1.
As illustrated in
As illustrated in
From the results, Test Example 1 in which the carrier having a specific surface area of 80 m2/g was used was capable of improving the maximum NO conversion rate more than Comparative Example 1 in which the carrier having a specific surface area of 300 m2/g was used by 10% or more.
In Test Example 2, a catalyst prepared in the same manner as in Test Example 1 except for the fact that titanium dioxide (TiO2) having a specific surface area of 21.3 m2/g was used as a carrier was used. In Test Example 3, a catalyst prepared in the same manner as in Test Example 1 except for the fact that titanium dioxide having a specific surface area of 14.2 m2/g was used as a carrier and the temperature in the activation step was set to 500° C. was used. In Test Example 4, a catalyst prepared in the same manner as in Test Example 1 except for the fact that the carrier of Test Example 3 was used was used. In Test Example 5, a catalyst prepared in the same manner as in Test Example 1 except for the fact that the carrier of Test Example 3 was used and the temperature and the time in the activation step were set to 600° C. and 20 hours was used. In Test Example 6, a catalyst prepared in the same manner as in Test Example 1 except for the fact that the carrier of Test Example 3 was used and the temperature and the time in the activation step were set to 600° C. and 50 hours was used. In Test Example 7, a catalyst prepared in the same manner as in Test Example 1 except for the fact that the carrier of Test Example 3 was used and the temperature and the time in the activation step were set to 800° C. and 20 hours was used. In Test Example 8, a catalyst prepared in the same manner as in Test Example 1 except for the fact that titanium dioxide having a specific surface area of 100 m2/g was used as a carrier was used.
In Comparative Example 2, a catalyst prepared in the same manner as in Test Example 1 except for the fact that the same carrier as Test Example 8 was used and the temperature and the time in the activation step were set to 800° C. and 50 hours was used.
Subsequently, denitration performance and CO oxidation performance of the catalysts of Test Examples 2 to 8 and Comparative Example 2 were measured in the same manner as in Test Example 1 and Comparative Example 1. In Test Examples 2 to 8 and Comparative Example 2, the catalyst layer inlet temperatures at which the NO conversion rate was maximized were, similar to Test Example 1 and Comparative Example 1, in a range of 250° C. to 270° C.
Subsequently, for Test Examples 1 to 8 ad Comparative Examples 1 and 2, crystallite diameters of metallic iridium in the catalysts were calculated from a diffraction angle and a full width at half maximum of a diffraction peak of a [111] plane using an X-ray diffraction method in which a powder X-ray diffraction device was used (X-ray source: Cu Kα1) using the Sherrer equation. In the following equation, D represents the crystallite diameter, K represents a constant (0.9), λ represents a wavelength of the X-ray source (in the case of Cu, 1.5405 angstrom), β represents the diffraction peak full width at half maximum (radian), and θ represents the diffraction angle.
D=K·λ/β·cos θ
Denitration performance in the case of using the denitration catalysts of Test Examples 1 to 8 and Comparative Examples 1 and 2 was measured. Table 2 shows compositions of the carriers, the specific surface areas of the carriers in the impregnation and supporting step, the specific surface areas of the denitration catalysts after the production of the catalysts, the conditions of the activation step, the crystallite diameters of metallic iridium, and the maximum NO conversion rates regarding Test Examples 1 to 8 and Comparative Examples 1 and 2.
As shown in Table 2 and
From the results, it was determined that an upper limit value of the specific surface area of the catalyst is set to 100 m2/g or less in order to set the maximum NO conversion rate to 60% or more. In addition, from the results of Test Example 1, it was determined that the upper limit value of the specific surface area of the catalyst is preferably set to 90 m2/g or less. Furthermore, from the results of Test Examples 2 to 7 and Comparative Example 2, it was confirmed that, when the upper limit value of the specific surface area of the catalyst is set to 68 m2/g or less, the maximum NO conversion rate can be set to 62% or more. In addition, from the results of Test Examples 3 to 7, it was confirmed that, a lower limit value of the specific surface area of the catalyst is preferably 12 m2/g or more.
From the results, it was determined that the crystallite diameter of the catalyst is set to 10 nm or more and 25 nm or less in order to set the maximum NO conversion rate to 60% or more. In addition, from the results of Test Examples 1 to 6, it was confirmed that, when the crystallite diameter of the catalyst is set to 10 nm or more and 23 nm or less, it is possible to set the maximum NO conversion rate to 64% or more. Furthermore, from the results of Test Examples 2 to 6, it was confirmed that, when the crystallite diameter of the catalyst is set to 12 nm or more and 23 nm or less, it is possible to set the maximum NO conversion rate to 65% or more.
In addition, as shown in Table 2, regarding the production methods of Test Examples 1 to 8 and Comparative Examples 1 and 2, in Test Example 1 in which the specific surface area of the carrier in the impregnation and supporting step was set to 80 m2/g, the maximum NO conversion rate was 64%. In Test Example 2 in which the specific surface area of the carrier was set to 21.3 m2/g, the maximum NO conversion rate was 71%. In Test Examples 3 to 7 in which the specific surface area of the carrier was set to 14.2 m2/g, the maximum NO conversion rates were 62 to 70%. In addition, in Test Example 8 in which the specific surface area of the carrier was set to 100 m2/g, the maximum NO conversion rate was 60%. On the other hand, in Comparative Example 1 in which the specific surface area of the carrier was set to 300 m2/g, the maximum NO conversion rate was 49%. In addition, in Comparative Example 2 in which the specific surface area of the carrier was set to 100 m2/g, the maximum NO conversion rate was 51%. In addition, as an effect of the production of the catalyst, the specific surface area of the carrier tends to decrease when a catalyst is produced.
From the results, it was determined that the upper limit value of the specific surface area of the carrier in the impregnation and supporting step is set to 100 m2/g or less in order to set the maximum NO conversion rate to 60% or more. In addition, from the results of Test Examples 1 to 7, it was confirmed that, when the upper limit value of the specific surface area of the carrier in the impregnation and supporting step is set to 80 m2/g or less, it is possible to set the maximum NO conversion rate to 62% or more. In addition, from the results of Test Examples 3 to 7, it was confirmed that the lower limit value of the specific surface area of the carrier in the impregnation and supporting step is preferably 14 m2/g or more.
In addition, from the results, it was confirmed that, as the conditions of the activation step, the activation temperature is preferably 500° C. or higher and 800° C. or lower, and the activation time is preferably 1 hour or longer and 50 hours or shorter. In addition, it was confirmed that, as the carrier in the impregnation and supporting step, TiO2 and/or SiO2 can be preferably employed.
CO oxidation capabilities in the case of using Test Examples 1 to 8 and Comparative Examples 1 and 2 as a CO oxidation catalyst were measured. Regarding Test Examples 1 to 8 and Comparative Examples 1 and 2, compositions of the carriers, the specific surface areas of the carriers in the impregnation and supporting step, the specific surface areas of the catalysts after the production of the catalysts, conditions of the activation step, the crystallite diameters of metallic iridium, the CO oxidation rates in a case in which the catalyst layer inlet temperature was 260° C. will be described.
As illustrated in
From the results, it was determined that the crystallite diameter of the catalyst is set to 10 nm or more and 23 nm or less in order to set the CO oxidation rate to 80% or more. In addition, from the results of Test Examples 2 to 6, it was confirmed that, when the crystallite diameter of the catalyst is set to 12 nm or more and 23 nm or less, the CO oxidation rate can be set to 85% or more.
In addition, from the results of Test Examples 1 to 6, it was confirmed that, as the conditions of the activation step, the activation temperature is preferably 500° C. or higher and 600° C. or lower, and the activation time is preferably 0.5 hours or longer and 50 hours or shorter. In addition, it was confirmed that, as the carrier in the impregnation and supporting step, TiO2 and/or SiO2 can be preferably employed.
According to the exhaust gas treatment catalyst, the method for producing an exhaust gas treatment catalyst, and the exhaust gas treatment system of the present invention, it is possible to improve the NO conversion rate in denitration using CO as a reducing agent. In addition, it is possible to improve the CO oxidation rate in the oxidation of CO in an exhaust gas.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2016-150470 | Jul 2016 | JP | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/JP2017/027374 | 7/28/2017 | WO | 00 |
