Patent Application
20220176349
The present invention relates to a denitration catalyst and a production method thereof.
In more detail, the present invention relates to a denitration catalyst used upon purifying exhaust gas produced by fuel combusting, and a production method thereof.
As one of the pollutants emitted into air by the combustion of fuel, nitrogen oxides (NO, NO2, NO3, N2O, N2O3, N2O4, N2O5) can be exemplified.
The nitrogen oxides induce acid rain, ozone layer depletion, photochemical smog, etc., and have a serious influence on the environment and human bodies; therefore, treatment thereof is an important problem.
As technology for removing the above-mentioned nitrogen oxides, the selective catalytic reduction reaction (NH3—SCR) with ammonia (NH3) as the reductant has been known.
As disclosed in Patent Document 1, a catalyst using titanium oxide as the carrier and supporting vanadium oxide is being widely used as the catalyst used in the selective catalytic reduction reaction.
Titanium oxide has low activity for sulfur oxides, and has high stability; therefore, it is best established as the carrier.
On the other hand, although vanadium oxide plays a main role in NH3—SCR, since it oxidizes SO2 to SO3, it has not been able to support on the order of 1 wt % or more of vanadium oxide.
In addition, with conventional NH3—SCR, since the catalyst made by supporting vanadium oxide on a titanium oxide carrier almost does not react at low temperature, it must be used at high temperatures such as 350 to 400° C.
However, in order to raise the degrees of freedom of design in devices and facilities realizing NH3—SCR and make more efficient, the development of a catalyst exhibiting high nitrogen oxide reduction rate activity at low temperatures has been demanded.
Subsequently, the present inventors have found a denitration catalyst in which vanadium pentoxide is present in at least 43 wt %, having a BET specific surface area of at least 30 m2/g, and which can be used in denitration at 200° C. or lower (Patent Document 2).
Patent Document 1: Japanese Unexamined Patent Application, Publication No. 2004-275852
Patent Document 2: Japanese Patent No. 6093101
The present inventors, as a result of thorough research trying to achieve a further improvement of the above Patent Document 2, found a denitration catalyst exhibiting a more superior reduction rate activity of nitrogen oxides.
The present invention has an object of providing a catalyst having better denitration efficiency at low temperature compared to the conventional technology, upon the selective catalytic reduction reaction with ammonia as the reductant.
The present invention relates to a denitration catalyst containing vanadium oxide, having a carbon content of at least 0.05 wt %, and having a defect site at which an oxygen deficiency occurs in the crystal structure.
In addition, in the denitration catalyst, having a defect site at which an oxygen deficiency occurs preferably indicates a ratio (P1/P2) of a peak intensity P2 of wavelength 494 to 549 cm−1 originating from edge-sharing 3V-Oc stretching vibration relative to a peak intensity P1 of wavelength 462 to 494 cm−1 originating from crosslinked V—OB—V bending vibration being 0.98 or less, in infrared transmission spectrum of the denitration catalyst.
In addition, the denitration catalyst is preferably used in denitration at 270° C. or lower.
In addition, the denitration catalyst preferably has an absorption edge wavelength of 575 nm or less.
In addition, the denitration catalyst preferably has a BET specific surface area of 15.3 m2/g or more.
In addition, the present invention relates to a production method for the denitration catalyst including a step of adding ethylene glycol to a precursor complex synthesized by mixing ammonium vanadate and oxalic acid, and then firing.
In addition, in the production method, a molar ratio of the oxalic acid to the ammonium vanadate is preferably at least 2.
A denitration catalyst according to the present invention has better denitration efficiency at low temperature compared to the conventional technology, upon the selective catalytic reduction reaction with ammonia as the reductant.
Hereinafter, embodiments of the present invention will be explained.
A denitration catalyst of the present invention is a denitration catalyst containing at least 43 wt % by vanadium pentoxide conversion of vanadium oxide, in which the carbon content is at least 0.05 wt %, and having a defect site at which an oxygen deficiency occurs in the crystal structure. Such a denitration catalyst can exhibit a high denitration effect even under a low temperature environment, compared to a denitration catalyst such as a vanadium/titanium catalyst which is conventionally used.
Firstly, the denitration catalyst of the present invention contains vanadium oxide.
This vanadium oxide includes vanadium oxide (II) (VO), vanadium trioxide (III) (V2O3), vanadium tetroxide (IV) (V2O4), and vanadium pentoxide (V) (V2O5), and the V element of vanadium pentoxide (V2O5) may assume the pentavalent, tetravalent, trivalent and divalent form in the denitration reaction.
It should be noted that this vanadium oxide is a main component of the denitration catalyst of the present invention, and may contain other substances within a range no inhibiting the effects of the present invention; however, it is preferably present in at least 50% by vanadium pentoxide conversion, in the denitration catalyst of the present invention.
More preferably, vanadium oxide is preferably present in at least 99% by vanadium pentoxide conversion, in the denitration catalyst of the present invention.
More preferably, vanadium oxide is preferably present at about 100% by vanadium pentoxide conversion, in the denitration catalyst of the present invention.
Secondly, the denitration catalyst of the present invention has a carbon content of at least 0.05 wt %, but can exhibit a high denitration effect even under a low temperature environment, compared to a denitration catalyst such as a vanadium/titanium catalyst which is conventionally used, by containing carbon in such a high concentration.
If impurities gets into the denitration catalyst of the present invention, the crystal structure is not continuous since the amorphous portion is produced in the denitration catalyst, a high denitration effect is exhibited by the lines and planes in the crystal lattice distorting; however, it is assumed that higher denitration effect is exhibited as carbon exists more abundantly as this impurities.
In the embodiment of the present invention, in the selective catalytic reduction reaction with a reaction temperature of 200° C. or less using the denitration catalyst having a carbon content of 0.07 wt %, it exhibited a NO conversion rate of 84.3% in the case of no moisture coexistence, and exhibited a NO conversion rate of 51.5% in the case of moisture coexisting.
In addition, in the selective catalytic reduction reaction using the denitration catalyst having a carbon content of 0.16 wt %, it exhibited a NO conversion rate of 100% in the case of no moisture coexistence, and exhibited a NO conversion rate of 60.1% in the case of moisture coexisting.
In addition, in the selective catalytic reduction reaction using the denitration catalyst having a carbon content of 0.17 wt %, it exhibited a NO conversion rate of 87.8% in the case of no moisture coexistence, and exhibited a NO conversion rate of 48.6% in the case of moisture coexisting.
On the other hand, in the selective catalytic reduction reaction using the denitration catalyst having a carbon content of 0.01 wt %, it only exhibited a NO conversion rate of 35.5% in the case of no moisture coexistence, and only exhibited a NO conversion rate of 5.2% in the case of moisture coexisting.
In addition, in the selective catalytic reduction reaction using the denitration catalyst having a carbon content of 0.04 wt %, it only exhibited a NO conversion rate of 39.2% in the case of no moisture coexistence, and only exhibited a NO conversion rate of 5.6% in the case of moisture coexisting.
In addition, in the aforementioned description, although it is stated as preferable for the carbon content in the denitration catalyst to be at least 0.05 wt %, it may more preferably have a carbon content of at least 0.07 wt %. More preferably, the carbon content may be at least 0.11 wt %. More preferably, the carbon content may be at least 0.12 wt %. More preferably, the carbon content may be at least 0.14 wt %. More preferably, the carbon content may be at least 0.16 wt %. More preferably, the carbon content may be at least 0.17 wt %.
Thirdly, the denitration catalyst of the present invention has a defect site at which oxygen deficiency occurs in the crystal structure.
It should be noted that, herein, “defect site” indicates being a position (site) at which a certain type of atom is not occupied, while being a position (site) which be occupied by this certain atom in the crystal.
In the above way, in the denitration catalyst of the present invention, the structure of the vanadium oxide crystal contained in this denitration catalyst is locally disordered due to mixing of impurities, and can exhibit high denitration effect; however, by impurities getting into the vanadium oxide catalyst of the present invention, it is assumed that a high denitration effect is exhibited by the sites at which oxygen atoms in the crystal structure are deficient appearing.
It should be noted that “site at which oxygen atoms are deficient” is also abbreviated as “oxygen defect site”.
It should be noted that, herein, “having a defect site at which oxygen deficiency occurs” refers to a ratio (P1/P2) of a peak intensity P2 of wavenumber 494 to 549 cm−1 originating from edge-sharing 3V—OC stretching vibration, relative to a peak intensity P1 of wavenumber 462 to 494 cm−1 originating from crosslinked V—OB—V bending vibration, in the infrared transmission spectrum of the denitration catalyst in the infrared transmission spectrum of the denitration catalyst, being no more than 0.98, after normalizing each spectrum with 1022 to 1016 cm−1 originated from terminal V═O stretching vibration in the infrared transmission spectrum of the denitration catalyst, as described in the Examples later. The wavenumber for calculating this “P1/P2” is the wavenumber in a case of the beginning to the end of the peak; however, in the case of calculating “P1/P2” using the wavenumber of the peak top, it may be calculated as the ratio of the peak intensity P2 of wavenumber 503 to 524 cm−1 originating from the edge-sharing 3V—OC stretching vibration, relative to the peak intensity P1 of wavenumbers 471 to 486 cm−1 originating from crosslinked V—OB—V bending vibration.
Furthermore, the denitration catalyst of the present invention may have a line defect in which point defects such as the “defect site at which an oxygen deficiency occurs” are continuously arranged one-dimensionally, a plane defect in which the point defects are continuously arranged two-dimensionally, or a lattice defect such as lattice strain, for example.
In addition, the denitration catalyst of the present invention is preferably used in denitration at 270° C. or lower. This is derived from the firing temperature of denitration catalyst of the present invention being 270° C.
On the other hand, in the Examples described later, the denitration catalyst of the present invention exhibits high denitration effect in the selective catalytic reduction reaction at the reaction temperature of 200° C. or lower, and thus the denitration catalyst of the present invention is capable of use in denitration at 200° C. or lower. During the selective catalytic reduction reaction, oxidation of SO2 to SO3 is thereby not accompanied, as in the knowledge obtained by the above Patent Document 2.
In addition, in the aforementioned disclosure, the denitration catalyst of the present invention is preferably used in denitration at 270° C. or lower; however, it may be preferably used in denitration at 200° C. or lower, and even more preferably, it may be used in denitration with a reaction temperature of 100 to 200° C.
More preferably, it may be used in denitration with a reaction temperature of 160 to 200° C.
Alternatively, it may be used in denitration with a reaction temperature of 80 to 150° C.
In addition, the absorption edge wavelength of the denitration catalyst of the present invention is preferably no more than 575 nm.
Generally, a higher denitration effect can be exhibited for catalyst in which the absorption edge wavelength is shifted more to the blue side in this way.
This is derived from the crystal structure collapsing as the absorption edge wavelength is shifted to the blue side.
In the embodiment of the present invention, for example, in the selective catalytic reduction reaction at the reaction temperature of 200° C. or lower, made using the denitration catalyst having an absorption edge wavelength of 567.4 nm, it exhibited a NO conversion rate of 61.3% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 28.1% in the case of coexisting with moisture.
In addition, in the selective catalytic reduction reaction using a denitration catalyst having an absorption edge wavelength of 548.2 nm, it exhibited a NO conversion rate of 84.3% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 51.5% in the case of coexisting with moisture.
In addition, with the selective catalytic reduction reaction using a denitration catalyst having an absorption edge wavelength of 547.7 nm, it exhibited a NO conversion rate of 79.2% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 50.6% in the case of coexisting with moisture.
In addition, with the selective catalytic reduction reaction using a denitration catalyst having an absorption edge wavelength of 535.9 nm, it exhibited a NO conversion rate of 87.8% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 48.6% in the case of coexisting with moisture.
In addition, with the selective catalytic reduction reaction using the denitration catalyst having an absorption edge wavelength of 534.5 nm, it exhibited a NO conversion rate of 100% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 60.1% in the case of coexisting with moisture.
On the other hand, with the selective catalytic reduction reaction using the denitration catalyst having an absorption edge wavelength of 587.3 nm, it only exhibited a NO conversion rate of 35.5% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 5.2% in the case of coexisting with moisture.
In addition, also with the selective catalytic reduction reaction using the denitration catalyst having an absorption edge wavelength of 580.1 nm, it only exhibited a NO conversion rate of 39.2% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 5.6% in the case of coexisting with moisture.
In addition, although the absorption edge wavelength of the denitration catalyst is no more than 575 nm, it may preferably be no more than 568 nm.
More preferably, it may be no more than 549 nm.
More preferably, it may be no more than 548 nm.
More preferably, it may be no more than 536 nm.
More preferably, it may be no more than 535 nm.
In addition, the BET specific surface area of the denitration catalyst of the present invention is preferably at least 15.3 m2/g; however, it exhibits higher denitration effect as the catalyst has larger BET specific surface area in this way.
It is assumed that this is because the number of sites which absorb more nitrogen oxides increases as the surface area per unit mass of denitration catalyst becomes larger.
In the embodiment of the present invention, with the selective catalytic reduction reaction at a reaction temperature of 200° C. or lower using a denitration catalyst having a BET specific surface area of 15.3 m2/g, it exhibited a NO conversion rate of 61.3% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 28.1% in the case of coexisting with moisture.
In addition, with the selective catalytic reduction reaction using a denitration catalyst having a BET specific surface area of 19.2 m2/g, it exhibited a NO conversion rate of 64.2% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 34.7% in the case of coexisting with moisture.
In addition, with the selective catalytic reduction reaction using a denitration catalyst having a BET specific surface area of 24.9 m2/g, it exhibited a NO conversion rate of 79.2% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 50.6% in the case of coexisting with moisture.
In addition, with the selective catalytic reduction reaction using a denitration catalyst having a BET specific surface area of 26.1 m2/g, it exhibited a NO conversion rate of 84.3% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 51.5% in the case of coexisting with moisture.
In addition, with the selective catalytic reduction reaction using a denitration catalyst having a BET specific surface area of 26.7 m2/g, it exhibited a NO conversion rate of 87.8% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 48.6% in the case of coexisting with moisture.
In addition, with the selective catalytic reduction reaction using a denitration catalyst having a BET specific surface area of 29.6 m2/g, it exhibited a NO conversion rate of 100% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 60.1% in the case of coexisting with moisture.
On the other hand, with the selective catalytic reduction reaction at the reaction temperature of 200° C. or lower using a denitration catalyst having a BET specific surface area of 15.2 m2/g, it only exhibited a NO conversion rate of 35.5% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 5.2% in the case of coexisting with moisture.
In addition, the BET specific surface area of the denitration catalyst is preferably at least 15.3 m2/g; however, it more preferably may be at least 19.2 m2/g.
More preferably, it may be at least 24.9 m2/g.
More preferably, the BET specific surface area of the denitration catalyst may be 26.1 m2/g.
More preferably, the BET specific surface area of the denitration catalyst may be at least 26.7 m2/g.
More preferably, the BET specific surface area of the denitration catalyst may be at least 29.6 m2/g.
It should be noted that the BET specific surface area of the denitration catalyst is preferably measured based on the criteria defined in JIS Z8830:2013.
The denitration catalyst containing at least 43 wt % of vanadium oxide by vanadium pentoxide conversion, and having carbon content of at least 0.05 wt %, and a defect site at which oxygen deficiency occurs in the crystal structure can be prepared by the sol gel method for the most part.
The sol gel method includes a step of firing after dissolving vanadate in a chelate compound and drying.
As the chelate compound, for example, that having a plurality of carboxyl groups such as oxalic acid and citric acid, that having a plurality of amino groups such as acetylacetonate and ethylenediamine, that having a plurality of hydroxyl groups such as ethylene glycol, etc. may be used.
In the embodiment of the present invention, a denitration catalyst produced by a method including a step of dissolving ammonium vanadate in oxalate solution, and a step of subsequently drying and firing exhibited a NO conversion rate of 64.2 to 100% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 20.9 to 60.1% in the case of coexisting with moisture.
In addition, a denitration catalyst produced by a method including a step of adding only ethylene glycol to ammonium vanadate and drying exhibited a NO conversion rate of 61.3% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 28.1% in the case of coexisting with moisture.
On the other hand, as the denitration catalyst produced by a method not including such a step, for example, a denitration catalyst obtained by firing only ammonium vanadate to make vanadium pentoxide, followed by adding only ethylene glycol and firing only exhibited a NO conversion rate of 35.5% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 5.2% in the case of coexisting with moisture.
In addition, a denitration catalyst obtained by firing only ammonium vanadate to make vanadium pentoxide, followed by adding oxalic acid and ethylene glycol and firing only exhibited a NO conversion rate of 39.2% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 5.6% in the case of coexisting with moisture.
In addition, the denitration catalyst of the present invention, in the embodiment, is produced by a method which adds ethylene glycol to a precursor complex synthesized by mixing ammonium vanadate and oxalic acid, and then firing. The denitration catalyst produced by such a method can exhibit a high denitration effect even under a low temperature environment, compared to a denitration catalyst such as a vanadium/titanium catalyst which is conventionally used. This is assumed to be because the carbon content in the denitration catalyst becomes high by adding ethylene glycol.
In the embodiment of the present invention, a denitration catalyst produced by a method of adding ethylene glycol to precursor complex synthesized by mixing ammonium vanadate and oxalic acid, and then firing exhibited a NO conversion rate of 64.2 to 100% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 34.7 to 60.1% in the case of coexisting with moisture.
On the other hand, for example, a denitration catalyst produced by a method of adding propylene glycol to precursor complex synthesized by mixing ammonium vanadate and oxalic acid, and then firing exhibited a NO conversion rate of 51.6% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 20.9% in the case of coexisting with moisture.
In addition, in the above-mentioned production method, the molar ratio of oxalic acid to the ammonium vanadate is at least 2.
The denitration catalyst produced by such a method can exhibit high denitration effect even under a low temperature environment, compared to a denitration catalyst such as a vanadium/titanium catalyst which is conventionally used. The matter of this originating from the vanadium pentoxide becoming higher specific surface area by adding oxalic acid serves as the reason.
In the above-mentioned production method according to the embodiment of the present invention, the denitration catalyst produced by a method in which the molar ratio of oxalic acid to ammonium vanadate becomes 2 exhibited a NO conversion rate of 84.3% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 51.5% in the case of coexisting with moisture.
In addition, the denitration catalyst produced by a method in which the molar ratio of oxalic acid to ammonium vanadate becomes 3 exhibited a NO conversion rate of 51.6 to 79.2% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 20.9 to 50.6% in the case of coexisting with moisture.
In addition, the denitration catalyst produced by a method in which the molar ratio of oxalic acid to ammonium vanadate becomes 6 exhibited a NO conversion rate of 64.2% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 34.7% in the case of coexisting with moisture.
In addition, the denitration catalyst produced by a method in which the molar ratio of oxalic acid to ammonium vanadate becomes 9 exhibited a NO conversion rate of 87.8% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 48.6% in the case of coexisting with moisture.
In addition, the denitration catalyst produced by a method in which the molar ratio of oxalic acid to ammonium vanadate becomes 15 exhibited a NO conversion rate of 100% in the case of not coexisting with moisture, and exhibited a NO conversion rate of 60.1% in the case of coexisting with moisture.
It should be noted that the above-mentioned sol gel method, although depending on the chelate compound, preferably includes a step of dissolving vanadate in oxalic acid, so that the molar ratio of vanadate and oxalic acid becomes 1:2 to 1:15, for example.
It should be noted that the molar ratio of vanadate and oxalic acid preferably may be 1:3 to 1:15.
More preferably, the molar ratio of vanadate and oxalic acid may be 1:6 to 1:15.
More preferably, the molar ratio of vanadate and oxalic acid may be 1:9 to 1:15.
More preferably, the molar ratio of vanadate and oxalic acid may be 1:15.
In the denitration catalyst prepared in this way, normally, vanadium oxide is contained, the carbon content is at least 0.05 wt %, and has a defect site at which oxygen deficiency occurs in the crystal structure.
According to the denitration catalyst related to the above-mentioned embodiment, the following effects are exerted.
(1) As mentioned above, the denitration catalyst according to the above embodiment contains vanadium oxide, has a carbon content of at least 0.05 wt %, and has a defect site in which an oxygen deficiency occurs in the crystal structure. By using this denitration catalyst, upon the selective catalytic reduction reaction with ammonia as the reductant, it is possible to exhibit an effect whereby the denitration efficiency is even higher at low temperature, compared to the conventional technology.
(2) As described above, regarding having a defect site at which the oxygen deficiency occurs in the denitration catalyst according to the above embodiment, the ratio (P1/P2) of the peak intensity P2 of wavenumbers 494 to 549 cm−1 originating from the originating from the edge-sharing 3V—OC stretching vibration, relative to the peak intensity P1 of wavenumbers 462 to 494 cm−1 originating from crosslinked V—OB—V bending vibration, in the infrared transmission spectrum of the denitration catalyst, is preferably no more than 0.98.
For the denitration catalyst according to the above embodiment, the adsorption of NO tends to occur, and can thereby exhibit higher NO conversion rate.
(3) As described above, the denitration catalyst according to the above embodiment is preferably used in denitration at 270° C. or less.
In the selective catalytic reduction reaction using the denitration catalyst according to the above embodiment, high denitration effect is brought about without causing the SO2 to oxidize.
(4) As described above, the denitration catalyst according to the above embodiment preferably has an absorption edge wavelength of 575 nm or less.
The denitration catalyst according to the above embodiment can thereby exhibit a NO conversion rate of 61.3% or more under conditions not coexisting with moisture.
(5) As described above, the denitration catalyst according to the above embodiment preferably has a BET specific surface area of 15.3 m2/g or more.
The denitration catalyst according to the above embodiment can thereby exhibit a NO conversion rate of 61.3% or more under conditions not coexisting with moisture.
(6) As described above, the production method of the denitration catalyst according to the above embodiment preferably includes a step of adding ethylene glycol to a precursor complex synthesized by adding oxalic acid to ammonium vanadate, and firing.
The carbon content of the denitration catalyst according to the above embodiment thereby becomes greater, and the denitration effect in the selective catalytic reduction reaction using the denitration catalyst according to the above embodiment improves.
(7) As described above, in the production method of the denitration catalyst according to the above embodiment, the molar ratio of oxalic acid to ammonium vanadate is preferably at least 2.
The carbon content of the denitration catalyst according to the above embodiment thereby becomes greater, and the denitration effect in the selective catalytic reduction reaction using the denitration catalyst according to the above embodiment improves.
It should be noted that the present invention is not to be limited to the above embodiment, and that modifications, improvements, etc. within a scope that can achieve the object of the present invention are also encompassed by the present invention.
Hereinafter, Examples of the present invention will be specifically explained together with Comparative Examples. It should be noted that the present invention is not limited to these Examples.
Ammonium vanadate was dissolved in an oxalic acid solution. Herein, the molar ratio of ammonium vanadate:oxalic acid is 1:3.
After completely dissolving, the moisture in the solution was evaporated on a hot stirrer, and was dried overnight at 120° C. in a dryer.
Subsequently, the dried powder was fired for 4 hours at 300° C. in air.
The fired vanadium pentoxide was established as the denitration catalyst of Comparative Example 1.
It should be noted the sample name of this denitration catalyst of Comparative Example 1 was set as “Va1ox3-0”.
It should be noted that this Comparative Example 1 is a denitration catalyst disclosed in the above Patent Document 2.
Ammonium vanadate (NH4VO3) and oxalic acid were dissolved in pure water.
After completely dissolving, the moisture in the solution was evaporated on a hot stirrer.
After mixing ethylene glycol with an oxalic acid-vanadium complex containing the prepared unreacted oxalic acid in an agate mortar for about 20 minutes, the denitration catalyst of vanadium pentoxide (V2O5) was obtained by twice firing at a temperature of 300° C. the obtained paste-like catalyst precursor by an electric oven.
Herein, the molar ratio of ammonium vanadate:oxalic acid:ethylene glycol is 1:3:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Example 1.
It should be noted that the sample name of this denitration catalyst of Example 1 was set as “Va1ox3-EG1”.
By the same method as Example 1, the denitration catalyst of vanadium pentoxide was obtained by adding triethylene glycol to the precursor complex synthesized by adding oxalic acid to ammonium vanadate, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:triethylene glycol is 1:3:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Comparative Example 2.
It should be noted that the sample name of this denitration catalyst of Comparative Example 2 was set as “Va1ox3-TG1”.
By the same method as Example 1, the denitration catalyst of vanadium pentoxide was obtained by adding butylene glycol to the precursor complex synthesized by adding oxalic acid to ammonium vanadate, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:butylene glycol is 1:3:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Comparative Example 3.
It should be noted that the sample name of this denitration catalyst of Comparative Example 3 was set as “Va1ox3-BG1”.
By the same method as Example 1, the denitration catalyst of vanadium pentoxide was obtained by adding propylene glycol to the precursor complex synthesized by adding oxalic acid to ammonium vanadate, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:propylene glycol is 1:3:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Comparative Example 4.
It should be noted that the sample name of this denitration catalyst of Comparative Example 4 was set as “Va1ox3-PG1”.
The denitration catalyst of vanadium pentoxide was obtained by adding only ethylene glycol to ammonium vanadate, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:propylene glycol is 1:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Example 2.
It should be noted that the sample name of this denitration catalyst of Example 2 was set as “Va1ox0-EG1”.
The denitration catalyst of vanadium pentoxide was obtained by firing only ammonium vanadate to make vanadium pentoxide, followed by adding only ethylene glycol, and then firing.
Herein, the molar ratio of ammonium vanadate:ethylene glycol is 1:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Comparative Example 5.
It should be noted that the sample name of this denitration catalyst of Comparative Example 5 was set as “V1ox0-EG1”.
The denitration catalyst of vanadium pentoxide was obtained by adding ethylene glycol to the precursor complex synthesized by adding oxalic acid to ammonium vanadate, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:ethylene glycol is 1:2:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Example 3.
It should be noted that the sample name of this denitration catalyst of Example 3 was set as “Va1ox2-EG1”.
The denitration catalyst of vanadium pentoxide was obtained by firing only ammonium vanadate to make vanadium pentoxide, followed by adding oxalic acid and ethylene glycol, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:ethylene glycol is 1:1:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Comparative Example 6.
It should be noted that the sample name of this denitration catalyst of Comparative Example 6 was set as “V1ox1-EG1”.
The denitration catalyst of vanadium pentoxide was obtained by adding ethylene glycol to the precursor complex synthesized by adding oxalic acid to ammonium vanadate, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:ethylene glycol is 1:6:2.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Example 4.
It should be noted that the sample name of this denitration catalyst of Example 4 was set as “Va1ox6-EG2”.
The denitration catalyst of vanadium pentoxide was obtained by adding ethylene glycol to the precursor complex synthesized by adding oxalic acid to ammonium vanadate, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:ethylene glycol is 1:9:3.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Example 5.
It should be noted that the sample name of this denitration catalyst of Example 5 was set as “Va1ox9-EG3”.
The denitration catalyst of vanadium pentoxide was obtained by adding ethylene glycol to the precursor complex synthesized by adding oxalic acid to ammonium vanadate, and then firing.
Herein, the molar ratio of ammonium vanadate:oxalic acid:ethylene glycol is 1:15:5.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Example 6.
It should be noted that the sample name of this denitration catalyst of Example 6 was set as “Va1ox15-EG5”.
The denitration catalyst of vanadium pentoxide was obtained by adding ethylene glycol to the precursor complex synthesized by adding oxalic acid to ammonium vanadate, and then firing, and synthesized so that carbon remained in the vanadium pentoxide.
Herein, the molar ratio of ammonium vanadate:oxalic acid:ethylene glycol is 1:1.8:1.
The vanadium pentoxide thereby obtained was defined as the denitration catalyst of Comparative Example 7.
It should be noted that the sample name of this denitration catalyst of Comparative Example 7 was set as “excess carbon”.
A Microtrac BEL BELSORP-max was used in the measurement of the BET specific surface area of each catalyst.
After pretreating for 2 hours at 200° C. under an Ar atmosphere, it was measured at 196° C.
Table 1 shows the BET specific surface areas of Examples 1 to 6, and Comparative Examples 1 to 6.
Except for Comparative Example 1 disclosed in Patent Document 2, a great difference was not found in the trend of values for BET specific surface area between the Examples and Comparative Examples.
More specifically, the example having the smallest BET specific surface area in the Examples was the value of 15.3 m2/g of Example 2, and the example having the largest BET specific surface area was the value of 29.6 m2/g of Example 6. On the other hand, the example having the smallest BET specific surface area in the Examples was the value of 15.2 m2/g of Example 5, and the example having the largest BET specific surface area other than Comparative Example 1 was the value of 26.0 m2/g of Comparative Example 3.
(Measurement Method 1) Under the conditions of Table 2 below, the NH3—SCR reaction was conducted using a fixed bed flow-type reactor at a reaction temperature of 100 to 200° C.
In the gas passing through the catalyst layer, NO was analyzed by a Jasco FT-IR-4700.
In addition, the NO conversion rate was calculated by Formula (1) noted below.
It should be noted that Noin is the NO concentration at the reaction tube inlet, and NOout is the NO concentration of the reaction tube outlet.
Table 3 shows the NO conversion rates of each vanadium pentoxide catalyst for both a case of moisture not coexisting and the case of coexisting with moisture.
For both the case of moisture not coexisting and the case of coexisting with moisture, the denitration catalysts of Examples generally showed a higher NO conversion rate than the denitration catalysts of the Comparative Examples. Above all, the denitration catalyst made by adding ethylene glycol as a precursor to ammonium vanadate and firing showed a high NO conversion rate.
Most importantly, Example 6 (Va1ox15-EG5) showed the highest NO conversion rate.
Under the conditions of Table 2 above, the NH3—SCR reaction was conducted by the same method as measurement method 1, at a plurality of reaction temperatures between 40° C. and 300° C. using the catalyst of Example 1 (Va1ox3-EG1).
As is evident from the graph of
It was thereby shown that denitration catalyst according to the Examples of the present invention are useful to an extent in denitration at approximately 80° C.
The reaction rate of NO was calculated by applying the NO conversion rates listed in Table 3, specific surface area of each catalyst listed in Table 1, etc. to Formula (2) below. Reaction rate [molNOmcat−1s−1]=conversion rate [%]×NO concentration (250 ppm)×flowrate (250 mL/min)/60/22400 [mL/mol]/catalyst amount (0.375 g)/specific surface area [m2/g] of each catalyst Formula (2)
It should be noted that, in Formula (2), “60” is the numerical value for converting minutes into seconds.
In both the case of moisture not coexisting and the case of coexisting with moisture, the denitration catalysts of the Examples generally showed higher conversion rates than the denitration catalysts of the Comparative Examples.
Above all, the denitration catalyst made by adding ethylene glycol to ammonium vanadate as a precursor, and then firing showed a high NO conversion rate.
Since the reaction rates per specific surface area of these catalysts are roughly close values, the precursor amount is assumed to contribute to variation in the specific surface area.
In addition, the reaction rates per specific surface area (activity) became values all higher than the Comparative Example 1, including for both the Examples and Comparative Examples.
Upon measurement of the carbon content of each vanadium pentoxide catalyst, the carbon content was quantified by elemental analysis of C (carbon), H (hydrogen) and N (nitrogen).
In more detail, in the reaction tube at high temperature inside of a CE-440F made by Exeter Analytical Inc., each denitration catalyst was completely combusted and decomposed to convert the C, H and N which are the main constituent elements into CO2, H2O and N2, followed by sequentially quantifying these three components in three thermal conductivity detectors to measure the contents of C, H and N in the constituent elements.
Table 4 shows the carbon content of each vanadium pentoxide catalyst.
According to the numerical values of Table 4, the carbon content included in the vanadium pentoxide catalysts of the Examples can be quantified as being at least 0.05 wt %.
For Example 1 (Va1ox3-EG1)), Example 2 (Va1ox0-EG1), Example 5 (Va1ox9-EG3) and Example 6 (Va1ox15-EG5) having a higher NO conversion rate than Comparative Example 1 (Va1ox3-0), it was shown that the carbon content exceeds 0.05 wt %.
Above all, in the case of moisture not coexisting, it was shown that the reaction rate per specific surface area became generally higher than Comparative Example 1 (Va1ox3-0) irrespective of the carbon content.
The ultraviolet and visible absorption spectrum of each vanadium pentoxide catalyst was measured.
Furthermore, in
In more detail, a sample of each vanadium pentoxide catalyst was filled into a sample holder including a white sheet of barium sulfate, and each ultraviolet and visible absorption spectrum was measured by the diffuse reflectance method. As the measuring apparatus, a UV-3100PC UV-visible spectrophotometer manufactured by Shimadzu was used.
Table 5 shows the absorption edge wavelength of each vanadium pentoxide catalyst.
According to Table 5, since the value of the absorption edge wavelength differed according to each vanadium pentoxide, it is assumed that the electronic structure differs according to the catalyst.
In addition, the highest absorption edge wavelength in the Examples is the 567.4 nm of Example 2 (Va1ox0-EG1). On the other hand, the highest absorption edge wavelength in the Comparative Examples is the 587.3 nm of Comparative Example 5 (V1ox0-EG1).
(Relationship between Absorption Edge Wavelength and Reaction Activity)
A trend was shown in which the NO conversion rate rises accompanying the absorption edge wavelength blue shifting, i.e. accompanying the crystal state collapsing.
A trend was shown in which the reaction rate per specific surface area rises accompanying the absorption edge wavelength blue shifting, i.e. accompanying the crystal state collapsing.
(Relationship between Absorption Edge Wavelength and BET Specific Surface Area)
Excluding Comparative Example 1 (Va1ox3-0), a great difference was not found in the BET specific surface areas, even when the absorption edge wavelength changed.
The infrared absorption spectrum of each vanadium pentoxide catalyst was measured.
In addition,
It should be noted that, upon measurement, a 1-mg sample of each vanadium pentoxide catalyst and 10 mg of potassium bromide were mixed, and then molded by pressurizing in a tablet molding machine.
Furthermore, the infrared absorption spectrum was measured by the transmission method using a TGS detector.
As the measurement apparatus, an FT/IR-6100 infrared spectrometer manufactured by JASCO Corporation was used.
As shown in
In the crystal structure, when the edge-sharing 3V-Oc is scarce and crosslinked V—OB—V is abundant, the absorption of NO tends to occur, and activity increases.
As shown in
From this matter, it is suggested to reflect the difference in structure of vanadium oxide for every catalyst.
Above all, this “P1/P2” corresponds to how much defect site at which the oxygen deficiency occurs is generating.
The infrared absorption spectra of
Table 6 shows the above transmittance ratios of Examples 1 to 6 and Comparative Examples 1 to 6.
The value of transmittance shown in Table 6 becomes smaller as the peaks in
For example, the transmittance of this peak becomes smaller as the peak on the low wavenumber side P1 (462 to 494 cm−1) returned to the crosslinked V—OB—V bulges out downwardly. According to Table 6, the ratio (P1/P2) of the peak intensity P2 relative to the peak intensity P1 of the Examples of the present invention can be quantified as 0.98 or less.
(Relationship between Infrared Absorption Spectrum and Catalyst Activity)
It is shown that the NO conversion rate rises together with a decrease in the ratio of transmittance.
From this fact, it is suggested that the activity improves as the proportion of edge-sharing 3V—OC becomes smaller.
It is shown that the reaction rate per specific surface area rises together with a decrease in transmittance ratio.
From this fact as well, it is suggested that the activity improves as the proportion of edge-sharing 3V—OC becomes smaller.
According to both graphs, the transmittance ratio of the Examples of the present invention can be quantified as 0.98 or less.
It should be noted that the above-mentioned transmittance ratio serves as an index of defect sites.
It should be noted that
On the other hand,
It should be noted that
As found from these images, there is no change in the morphology from the presence/absence of addition of ethylene glycol.
For Comparative Example 1 (Va1ox3-0), Example 1 (Va1ox3-EG1), Comparative Example 2 (Va1ox3-TG1), Comparative Example 3 (Va1ox3-BG1), and Comparative Example 4 (Va1ox3-PG1), the X-ray photoelectron spectrum (XPS) was measured in order to analyze the electronic state.
In more detail, powder samples of each catalyst of the Examples and Comparative Examples were fixed to a sample holder using carbon tape, and the X-ray photoelectron spectrum was measured.
As the measurement device, a JPS-9010MX photoelectron spectrometer manufactured by JEOL Ltd. was used.
A clear change in electronic state for every catalyst was not confirmed.
Adsorption isotherms were obtained for Examples 1 to 6 and Comparative Examples 1 to 6.
In other words, the equilibrium adsorption amount of water adsorbed to each catalyst under constant temperature was measured while changing the relative pressure.
More specifically, powder of the catalyst of each Example and each Comparative Example was encapsulated in a sample holder, and measurement was performed using a Belsorp-maxk manufactured by BELCAT.
It should be noted that, herein, “relative pressure” indicates a ratio of the adsorption equilibrium pressure relative to the saturated vapor pressure, and is a value of 0 to 1.
In both
(Relationship between Water Adsorption Amount and Catalyst Activity)
A correlation between the water adsorption amount and NO conversion rate was not found.
A correlation between the water adsorption amount and reaction rate per specific surface area was not found.
In order to analyze the crystal structure of each vanadium pentoxide catalyst, the Raman spectra was measured by Raman spectroscopy.
From
On the other hand, the peak originating from the defect mode, etc. did not appear.
In the above way, for a denitration catalyst containing at least 43 wt % vanadium oxide by vanadium pentoxide conversion, and having a carbon content of at least 0.05 wt %, the denitration efficiency at a low temperature of 270° C. or lower is high in the selective catalytic reduction reaction with ammonia as the reductant, using the denitration catalyst of the present invention having a defect site at which the oxygen deficiency occurs in the crystal structure.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/JP2019/009199 | 3/7/2019 | WO | 00 |
