U.S. patent application number 15/764038 was filed with the patent office on 2018-09-27 for denitration catalyst and method for producing the same.
The applicant listed for this patent is The Chugoku Electric Power Co., Inc., Tokyo Metropolitan University. Invention is credited to Masatake HARUTA, Kenji HIKINO, Eiji KIYONAGA, Makoto MINO, Keiichiro MORITA, Toru MURAYAMA.
Application Number | 20180272318 15/764038 |
Document ID | / |
Family ID | 58261857 |
Filed Date | 2018-09-27 |
United States Patent
Application |
20180272318 |
Kind Code |
A1 |
KIYONAGA; Eiji ; et
al. |
September 27, 2018 |
DENITRATION CATALYST AND METHOD FOR PRODUCING THE SAME
Abstract
There is provided a catalyst that exhibits a high denitration
efficiency at a relatively low temperature and does not cause
oxidation of SO.sub.2 in a selective catalytic reduction reaction
that uses ammonia as a reducing agent. A denitration catalyst
contains 3.3 wt % or more of vanadium oxide in terms of vanadium
pentoxide and has a BET specific surface area of 10 m.sup.2/g or
more.
Inventors: |
KIYONAGA; Eiji; (Hiroshima,
JP) ; HIKINO; Kenji; (Hiroshima, JP) ; MORITA;
Keiichiro; (Hiroshima, JP) ; HARUTA; Masatake;
(Tokyo, JP) ; MURAYAMA; Toru; (Tokyo, JP) ;
MINO; Makoto; (Tokyo, JP) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
The Chugoku Electric Power Co., Inc.
Tokyo Metropolitan University |
Hiroshima
Tokyo |
|
JP
JP |
|
|
Family ID: |
58261857 |
Appl. No.: |
15/764038 |
Filed: |
September 12, 2016 |
PCT Filed: |
September 12, 2016 |
PCT NO: |
PCT/JP2016/076870 |
371 Date: |
March 28, 2018 |
Current U.S.
Class: |
1/1 |
Current CPC
Class: |
F01N 3/021 20130101;
Y02E 20/12 20130101; B01J 37/0009 20130101; F01N 3/2066 20130101;
F01N 3/2842 20130101; B01D 2251/206 20130101; B01J 37/036 20130101;
B01J 38/485 20130101; F01N 5/02 20130101; B01D 53/9436 20130101;
B01D 2255/20723 20130101; B01D 2259/4566 20130101; B01J 37/0219
20130101; B01J 38/66 20130101; F01N 3/0205 20130101; F01N 13/009
20140601; B01J 38/64 20130101; B01D 53/8628 20130101; F01N 2510/068
20130101; B01D 2255/20707 20130101; B01J 35/1014 20130101; B01J
37/082 20130101; B01J 35/002 20130101; F01N 2370/02 20130101; B01D
53/90 20130101; B01D 53/96 20130101; F01N 3/208 20130101; B01J
38/02 20130101; Y02T 10/12 20130101; B01J 37/08 20130101; B01D
2255/9207 20130101; F01N 3/28 20130101; B01D 2258/012 20130101;
B01J 23/22 20130101; B01J 37/088 20130101; F01N 2330/06 20130101;
F01N 2590/02 20130101; F01N 2330/08 20130101; F01N 2330/42
20130101; F01N 2570/14 20130101; F01N 2330/00 20130101; B01J 23/92
20130101; F01N 3/2803 20130101; F01N 2610/02 20130101; Y02A 50/20
20180101; B01D 53/9418 20130101 |
International
Class: |
B01J 23/22 20060101
B01J023/22; B01J 35/10 20060101 B01J035/10; B01J 37/08 20060101
B01J037/08; B01D 53/94 20060101 B01D053/94; F01N 3/20 20060101
F01N003/20 |
Claims
1. A denitration catalyst comprising 3.3 wt % or more of vanadium
oxide in terms of vanadium pentoxide, wherein the denitration
catalyst has a BET specific surface area of 10 m2/g or more.
2. The denitration catalyst according to claim 1, wherein the
denitration catalyst is used for denitration at 200.degree. C. or
lower.
3. The denitration catalyst according to claim 1, wherein an amount
of NH3 desorbed by NH3-TPD (TPD: temperature programed desorption)
is 10.0 mmol/g or more.
4. A method for producing the denitration catalyst according to
claim 1, the method comprising a step of thermally decomposing a
vanadate at a temperature of 300.degree. C. to 400.degree. C.
5. A method for producing the denitration catalyst according to
claim 1, the method comprising a step of dissolving a vanadate in a
chelate compound, performing drying, and then performing firing.
Description
TECHNICAL FIELD
[0001] The present invention relates to a denitration catalyst and
a method for producing the denitration catalyst. More specifically,
the present invention relates to a denitration catalyst used when
exhaust gas generated through fuel combustion is cleaned up and a
method for producing the denitration catalyst.
BACKGROUND ART
[0002] One of pollutants emitted to the air through fuel combustion
is nitrogen oxide (NO, NO.sub.2, NO.sub.3, N.sub.2O,
N.sub.2O.sub.3, N.sub.2O.sub.4, or N.sub.2O.sub.5). Nitrogen oxide
causes, for example, acid rain, ozone depletion, and photochemical
smog and seriously affects the environment and the human body, and
therefore the treatment for nitrogen oxide has been an important
issue.
[0003] A known technique of removing the nitrogen oxide is a
selective catalytic reduction reaction (NH.sub.3-SCR) that uses
ammonia (NH.sub.3) as a reducing agent. As described in Patent
Document 1, a catalyst in which vanadium oxide is supported on
titanium oxide serving as a carrier is widely used as a catalyst
for the selective catalytic reduction reaction. Titanium oxide is
the best carrier because titanium oxide has a low activity against
sulfur oxide and has high stability. [0004] Patent Document 1:
Japanese Unexamined Patent Application, Publication No.
2004-275852
DISCLOSURE OF THE INVENTION
Problems to be Solved by the Invention
[0005] On the other hand, vanadium oxide plays a key role in the
NH.sub.3-SCR, but vanadium oxide cannot be supported in an amount
of about 1 wt % or more because vanadium oxide oxidizes SO.sub.2
into SO.sub.3. Therefore, vanadium oxide is typically used in an
amount of 1 wt % or less relative to its carrier. Furthermore, in
the current NH.sub.3-SCR, a catalyst in which vanadium oxide (and
tungsten oxide in some cases) is supported on a titanium oxide
carrier hardly reacts at low temperature and thus needs to be used
at a high temperature of 350.degree. C. to 400.degree. C.
[0006] In order to increase the degree of freedom in the design of
apparatuses and facilities with which the NH.sub.3-SCR is performed
and increase the efficiency, the development of a catalyst having a
high nitrogen oxide reduction activity even at low temperature has
been demanded.
[0007] In view of the foregoing, it is an object of the present
invention to provide a catalyst that exhibits a high denitration
efficiency at low temperature and does not cause oxidation of
SO.sub.2 in a selective catalytic reduction reaction that uses
ammonia as a reducing agent.
Means for Solving the Problems
[0008] The present invention relates to a denitration catalyst
containing 3.3 wt % or more of vanadium oxide in terms of vanadium
pentoxide and having a BET specific surface area of 10 m.sup.2/g or
more.
[0009] The denitration catalyst is preferably used for denitration
at 200.degree. C. or lower.
[0010] In the denitration catalyst, an amount of NH.sub.3 desorbed
by NH.sub.3-TPD (TPD: temperature programed desorption) is
preferably 10.0 mmol/g or more.
[0011] The present invention relates to a method for producing the
denitration catalyst, the method including a step of thermally
decomposing a vanadate at a temperature of 300.degree. C. to
400.degree. C.
[0012] The present invention relates to a method for producing the
denitration catalyst, the method including a step of dissolving a
vanadate in a chelate compound, performing drying, and then
performing firing.
Effects of the Invention
[0013] The denitration catalyst according to the present invention
exhibits a high denitration efficiency particularly at 200.degree.
C. or lower, which allows detoxification of NO into N.sub.2. The
selective catalytic reduction reaction that uses the denitration
catalyst according to the present invention can be performed at
200.degree. C. or lower, and therefore oxidation of SO.sub.2 does
not occur.
BRIEF DESCRIPTION OF THE DRAWINGS
[0014] FIG. 1 illustrates the powder X-ray diffraction results of
vanadium pentoxide catalysts produced in Examples 1 to 3 and
Comparative Example 1.
[0015] FIG. 2 illustrates the powder X-ray diffraction results of
vanadium pentoxide catalysts produced in Examples 3 to 8 and
Comparative Examples 2 and 3.
[0016] FIG. 3 illustrates the NH.sub.3-SCR activity of vanadium
pentoxide catalysts produced in Examples 1 to 3 and Comparative
Examples 1 and 4.
[0017] FIG. 4 illustrates the relationship between the reaction
temperature and the N.sub.2 selectivity in a selective catalytic
reduction reaction that uses vanadium pentoxide catalysts produced
in Example 1 and Comparative Example 1.
[0018] FIG. 5 illustrates the space velocity dependency in the case
where a vanadium pentoxide catalyst produced in Example 1 is used
in a NH.sub.3-SCR reaction.
[0019] FIG. 6 illustrates a change in the NO conversion ratio over
time in the case where a vanadium pentoxide catalyst produced in
Example 1 is used in a selective catalytic reduction reaction in
coexistence with water.
[0020] FIG. 7 illustrates changes in the NH.sub.3, NO, and SO.sub.2
concentrations over time in the case where a vanadium pentoxide
catalyst produced in Example 1 is used in a selective catalytic
reduction reaction in coexistence with S.
[0021] FIG. 8 illustrates the relationship between the amount of
vanadium pentoxide supported and the NO conversion ratio of a
vanadium pentoxide catalyst produced in each of Examples at each
reaction temperature.
[0022] FIG. 9 illustrates the relationship between the BET specific
surface area and the NO conversion ratio of a vanadium pentoxide
catalyst produced in each of Examples and Comparative Examples.
[0023] FIG. 10 illustrates the powder X-ray diffraction results of
vanadium pentoxide catalysts produced in Examples 10 to 14.
[0024] FIG. 11 illustrates the NH.sub.3-SCR activity of vanadium
pentoxide catalysts produced in Examples 10 to 14.
[0025] FIG. 12 illustrates the relationship between the specific
surface area and the NO conversion ratio of vanadium pentoxide
catalysts in Examples 1 and 2, Examples 10 to 13, and Comparative
Example 1.
[0026] FIG. 13 illustrates the relationship between the BET
specific surface area and the amount of NH.sub.3 desorbed of
vanadium pentoxide catalysts produced in Examples 1 and 2, Examples
11 and 12, and Comparative Example 1.
[0027] FIG. 14 illustrates the relationship between the amount of
NH.sub.3 desorbed and the NO conversion ratio of vanadium pentoxide
catalysts produced in Examples 1 and 2, Examples 11 and 12, and
Comparative Example 1.
PREFERRED MODE FOR CARRYING OUT THE INVENTION
[0028] Hereafter, embodiments of the present invention will be
described.
[0029] A denitration catalyst of the present invention contains 3.3
wt % or more of vanadium oxide in terms of vanadium pentoxide and
has a BET specific surface area of 10 m.sup.2/g or more. Such a
denitration catalyst can exhibit a high denitration effect even in
a low-temperature environment compared with known denitration
catalysts such as a vanadium/titanium catalyst.
[0030] Specifically, when a denitration catalyst containing 3.3 wt
% or more of vanadium oxide in terms of vanadium pentoxide is used
in a selective catalytic reduction reaction (NH.sub.3-SCR) that
uses ammonia as a reducing agent, the NO conversion ratio is
approximately 35% or more at a reaction temperature of 120.degree.
C. and approximately 60% or more at a reaction temperature of
150.degree. C. Even at a reaction temperature of 100.degree. C.,
the NO conversion ratio exceeds 20%. In contrast, if the
denitration catalyst contains only less than 3.3 wt % of vanadium
oxide in terms of vanadium pentoxide, the NO conversion ratio is
less than 20% at a reaction temperature of 120.degree. C. and even
at a reaction temperature of 150.degree. C.
[0031] As described above, the denitration catalyst according to
the present invention contains 3.3 wt % or more of vanadium oxide
in terms of vanadium pentoxide, and may also contain titanium oxide
as another component in addition to the vanadium oxide.
Furthermore, a noble metal, a base metal, and a main group metal
may be contained. Preferably, for example, tungsten oxide, chromium
oxide, and molybdenum oxide can also be contained.
[0032] It has been described that the denitration catalyst
preferably contains 3.3 wt % or more of vanadium oxide in terms of
vanadium pentoxide. Preferably, the denitration catalyst may
contain 9 wt % or more of vanadium oxide in terms of vanadium
pentoxide. More preferably, the denitration catalyst may contain 20
wt % or more of vanadium oxide in terms of vanadium pentoxide. More
preferably, the denitration catalyst may contain 33 wt % or more of
vanadium oxide in terms of vanadium pentoxide. More preferably, the
denitration catalyst may contain 43 wt % or more of vanadium oxide
in terms of vanadium pentoxide. More preferably, the denitration
catalyst may contain 80 wt % or more of vanadium oxide in terms of
vanadium pentoxide. More preferably, the content of vanadium oxide
in the denitration catalyst may be 100%.
[0033] The above-described vanadium oxide includes vanadium(II)
oxide (VO), vanadium(III) trioxide (V.sub.2O.sub.5), vanadium(IV)
dioxide (V.sub.2O.sub.4), and vanadium(V) pentoxide
(V.sub.2O.sub.5), and the V element in vanadium pentoxide
(V.sub.2O.sub.5) may have a pentavalent, tetravalent, trivalent, or
divalent form in the denitration reaction.
[0034] Regarding the BET specific surface area of the denitration
catalyst, for example, in the NH.sub.3-SCR that is performed at a
reaction temperature of 120.degree. C. using a denitration catalyst
containing vanadium pentoxide and having a BET specific surface
area of 13.5 m.sup.2 g.sup.-1, the NO conversion ratio exceeds 20%.
Even in the NH.sub.3-SCR that is performed at a reaction
temperature of 120.degree. C. using a denitration catalyst
containing vanadium pentoxide and having a BET specific surface
area of 16.6 m.sup.2 g.sup.-1, the NO conversion ratio exceeds 20%.
In contrast, in the NH.sub.3-SCR that is performed at a reaction
temperature of 120.degree. C. using, for example, a denitration
catalyst having a BET specific surface area of 4.68 m.sup.2/g,
which is a denitration catalyst having a BET specific surface area
of less than 10 m.sup.2/g, the NO conversion ratio falls below
20%.
[0035] The BET specific surface area of the denitration catalyst is
10 m.sup.2/g or more and may be preferably 15 m.sup.2/g or more.
More preferably, the BET specific surface area of the denitration
catalyst may be 30 m.sup.2/g. More preferably, the BET specific
surface area of the denitration catalyst may be 40 m.sup.2/g or
more. More preferably, the BET specific surface area of the
denitration catalyst may be 50 m.sup.2/g or more. More preferably,
the BET specific surface area of the denitration catalyst may be 60
m.sup.2/g or more.
[0036] The BET specific surface area of the denitration catalyst is
preferably measured in conformity with the conditions specified in
JIS Z 8830:2013. Specifically, the BET specific surface area can be
measured by a method described in Examples below.
[0037] The denitration catalyst of the present invention is used
for denitration at 200.degree. C. or lower. Preferably, the
denitration catalyst is used for denitration at 160.degree. C. or
higher and 200.degree. C. or lower. Thus, oxidation of SO.sub.2
into SO.sub.3 does not occur during the NH.sub.3-SCR reaction.
[0038] Regarding the amount of NH.sub.3 desorbed by NH.sub.3-TPD
(TPD: temperature programed desorption), when the amount of
NH.sub.3 desorbed exceeds 10.0 mmol/g, the NO conversion ratio of
the denitration catalyst in the NH.sub.3-SCR at a reaction
temperature of 120.degree. C. is 20% or more. In contrast, when the
amount of NH.sub.3 desorbed falls below 10.0 mmol/g, the NO
conversion ratio of the denitration catalyst in the NH.sub.3-SCR at
a reaction temperature of 120.degree. C. falls below 20%.
[0039] In the denitration catalyst of the present invention, the
amount of NH.sub.3 desorbed by NH.sub.3-TPD (TPD: temperature
programed desorption) is 10.0 mmol/g or more. Preferably, the
amount of NH.sub.3 desorbed by NH.sub.3-TPD may be 20.0 mmol/g or
more. More preferably, the amount of NH.sub.3 desorbed by
NH.sub.3-TPD may be 50.0 mmol/g or more. More preferably, the
amount of NH.sub.3 desorbed by NH.sub.3-TPD may be 70.0 mmol/g or
more.
[0040] The denitration catalyst containing 3.3 wt % or more of
vanadium oxide in terms of vanadium pentoxide and having a BET
specific surface area of 10 m.sup.2/g or more can be produced by
any of a thermal decomposition process, a sol-gel process, and an
impregnation process. Hereafter, a method for producing the
denitration catalyst containing 3.3 wt % or more of vanadium
pentoxide and having a specific surface area of 10 m.sup.2/g or
more by a thermal decomposition process, a sol-gel process, or an
impregnation process will be described.
[0041] The thermal decomposition process includes a step of
thermally decomposing a vanadate. Examples of the vanadate that may
be used include ammonium vanadate, magnesium vanadate, strontium
vanadate, barium vanadate, zinc vanadate, tin vanadate, and lithium
vanadate.
[0042] In the thermal decomposition process, the vanadate is
preferably thermally decomposed at 300.degree. C. to 400.degree.
C.
[0043] The sol-gel process includes a step of dissolving a vanadate
in a chelate compound, performing drying, and performing firing.
Examples of the chelate compound that may be used include compounds
having a plurality of carboxy groups, such as oxalic acid and
citric acid; compounds having a plurality of amino groups, such as
acetylacetonate and ethylenediamine; and compounds having a
plurality of hydroxy groups, such as ethylene glycol.
[0044] The sol-gel process preferably includes a step of dissolving
a vanadate in a chelate compound such that the molar ratio of
vanadium and the chelate compound is, for example, 1:1 to 1:5,
though this is dependent on the chelate compound. Preferably, the
molar ratio of the vanadate and the chelate compound may be 1:2 to
1:4.
[0045] The impregnation process includes a step of dissolving a
vanadate in a chelate compound, adding a carrier, performing
drying, and then performing firing. Examples of the carrier that
may be used include titanium oxide, aluminum oxide, and silica. As
above, examples of the chelate compound that may be used include
compounds having a plurality of carboxy groups, such as oxalic acid
and citric acid; compounds having a plurality of amino groups, such
as acetylacetonate and ethylenediamine; and compounds having a
plurality of hydroxy groups, such as ethylene glycol.
[0046] In the impregnation process, xwt % V.sub.2O.sub.5/TiO.sub.2
(x.gtoreq.9) may be produced as a denitration catalyst according to
an embodiment of the present invention by, for example, dissolving
ammonium vanadate in an oxalic acid solution, adding titanium oxide
(TiO.sub.2) serving as a carrier, performing drying, and then
performing firing.
[0047] The thus-produced denitration catalyst normally contains 3.3
wt % or more of vanadium pentoxide and has a specific surface area
of 10 m.sup.2/g or more.
[0048] The denitration catalyst according to the above embodiment
produces the following effects.
[0049] (1) As described above, the denitration catalyst according
to the above embodiment contains 3.3 wt % or more of vanadium oxide
in terms of vanadium pentoxide and has a specific surface area of
10 m.sup.2/g or more. By using this denitration catalyst, a high
denitration effect can be produced even in a selective catalytic
reduction reaction at 200.degree. C. or lower.
[0050] (2) As described above, the denitration catalyst according
to the above embodiment is preferably used for denitration at
200.degree. C. or lower. This produces a high denitration effect in
the selective catalytic reduction reaction that uses the
denitration catalyst according to the above embodiment without
oxidizing SO.sub.2.
[0051] (3) As described above, in the denitration catalyst
according to the above embodiment, the amount of NH.sub.3 desorbed
by NH.sub.3-TPD (TPD: temperature programed desorption) is
preferably 10.0 mmol/g or more. When this denitration catalyst is
used in the NH.sub.3-SCR at a reaction temperature of 120.degree.
C., the NO conversion ratio exceeds 20%.
[0052] (4) As described above, the method for producing a
denitration catalyst according to the above embodiment preferably
includes a step of thermally decomposing a vanadate at 300.degree.
C. to 400.degree. C. This increases the specific surface area of
the denitration catalyst according to the above embodiment, which
improves a denitration effect in the selective catalytic reduction
reaction that uses the denitration catalyst according to the above
embodiment.
[0053] (5) As described above, the method for producing a
denitration catalyst according to the above embodiment preferably
includes a step of dissolving a vanadate in a chelate compound,
performing drying, and then performing firing. This increases the
specific surface area of the denitration catalyst according to the
above embodiment, which improves a denitration effect in the
selective catalytic reduction reaction that uses the denitration
catalyst according to the above embodiment.
[0054] The present invention is not limited to the above
embodiment, and any of modifications, improvements, and the like
are included in the present invention as long as the object of the
present invention is achieved.
EXAMPLES
[0055] Hereafter, Examples of the present invention will be
specifically described together with Comparative Examples. The
present invention is not limited by Examples.
1. Relationship Between Vanadium Oxide Content and Specific Surface
Area in Catalyst and NH.sub.3-SCR Activity
1.1 Examples and Comparative Examples
Example 1
[0056] Ammonium vanadate (NH.sub.4VO.sub.3) was thermally
decomposed in the air at 300.degree. C. for 4 hours to obtain
vanadium pentoxide (V.sub.2O.sub.5). The obtained vanadium
pentoxide was used as a denitration catalyst in Example 1. The
sample name of the denitration catalyst in Example 1 was
"V.sub.2O.sub.5.sub._300".
Example 2
[0057] Ammonium vanadate was thermally decomposed in the air at
400.degree. C. for 4 hours to obtain vanadium pentoxide. The
obtained vanadium pentoxide was used as a denitration catalyst in
Example 2. The sample name of the denitration catalyst in Example 2
was "V.sub.2O.sub.5.sub._400".
Comparative Example 1
[0058] Ammonium vanadate was thermally decomposed in the air at
500.degree. C. for 4 hours to obtain vanadium pentoxide. The
obtained vanadium pentoxide was used as a denitration catalyst in
Comparative Example 1. The sample name of the denitration catalyst
in Comparative Example 1 was "V.sub.2O.sub.5.sub._500".
Example 3
[0059] Ammonium vanadate was dissolved in an oxalic acid solution
(molar ratio of vanadium:oxalic acid=1:3). After ammonium vanadate
was completely dissolved, water in the solution was evaporated on a
hot stirrer, and drying was performed in a dryer at 120.degree. C.
for one night. Then, the dried powder was fired in the air at
300.degree. C. for 4 hours. The vanadium pentoxide after firing was
used as a denitration catalyst in Example 3. The sample name of the
denitration catalyst in Example 3 obtained by this sol-gel process
was "V.sub.2O.sub.5.sub._SG_300". Denitration catalysts obtained at
different molar ratios of vanadium and oxalic acid when ammonium
vanadate is dissolved in an oxalic acid solution will be described
later.
Comparative Example 2
[0060] Ammonium vanadate was added to an oxalic acid solution and
stirred for 10 minutes, and titanium oxide serving as a carrier was
gradually added. Then, water in the solution was evaporated on a
hot stirrer and drying was performed in a dryer at 120.degree. C.
for one night. Subsequently, the dried powder was fired in the air
at 300.degree. C. for 4 hours. As a result, the denitration
catalyst after firing that contained 0.3 wt % of vanadium pentoxide
was used as a denitration catalyst in Comparative Example 2. The
sample name of the denitration catalyst in Comparative Example 3
was "0.3 wt % V.sub.2O.sub.5/TiO.sub.2".
Comparative Example 3
[0061] The denitration catalyst after firing that was obtained by
the same method as in Comparative Example 2 and contained 0.9 wt %
of vanadium pentoxide was used as a denitration catalyst in
Comparative Example 3. The sample name of the denitration catalyst
in Comparative Example 4 was "0.9 wt %
V.sub.2O.sub.5/TiO.sub.2".
Example 4
[0062] The denitration catalyst after firing that was obtained by
the same method as in Comparative Example 2 and contained 3.3 wt %
of vanadium pentoxide was used as a denitration catalyst in Example
4. The sample name of the denitration catalyst in Example 4 was
"3.3 wt % V.sub.2O.sub.5/TiO.sub.2".
Example 5
[0063] The denitration catalyst after firing that was obtained by
the same method as in Comparative Example 2 and contained 9 wt % of
vanadium pentoxide was used as a denitration catalyst in Example 5.
The sample name of the denitration catalyst in Example 5 was "9 wt
% V.sub.2O.sub.5/TiO.sub.2".
Example 6
[0064] The denitration catalyst after firing that was obtained by
the same method as in Comparative Example 2 and contained 20 wt %
of vanadium pentoxide was used as a denitration catalyst in Example
6. The sample name of the denitration catalyst in Example 5 was "20
wt % V.sub.2O.sub.5/TiO.sub.2".
Example 7
[0065] The denitration catalyst after firing that was obtained by
the same method as in Comparative Example 2 and contained 33 wt %
of vanadium pentoxide was used as a denitration catalyst in Example
7. The sample name of the denitration catalyst in Example 7 was "33
wt % V.sub.2O.sub.5/TiO.sub.2".
Example 8
[0066] The denitration catalyst after firing that was obtained by
the same method as in Comparative Example 2 and contained 43 wt %
of vanadium pentoxide was used as a denitration catalyst in Example
8. The sample name of the denitration catalyst in Example 8 was "43
wt % V.sub.2O.sub.5/TiO.sub.2".
Example 9
[0067] The denitration catalyst after firing that was obtained by
the same method as in Comparative Example 2 and contained 80 wt %
of vanadium pentoxide was used as a denitration catalyst in Example
9. The sample name of the denitration catalyst in Example 9 was "80
wt % V.sub.2O.sub.5/TiO.sub.2".
Comparative Example 4
[0068] An existing catalyst was used in Comparative Example 4. The
existing catalyst is a catalyst in which, for example, tungsten
oxide (WO.sub.3) (content: 10.72 wt %) and silica (SiO.sub.2)
(content: 6.25 wt %) are supported on titanium oxide (TiO.sub.2)
(content: 79.67 wt %) and which contains about 0.5% of
vanadium.
1.2 Evaluation
1.2.1 Powder X-Ray Diffraction
(Diffraction Method)
[0069] Powder X-ray diffraction analysis was performed with a
Rigaku smart lab using Cu-Ka.
(Diffraction Result)
[0070] FIG. 1 illustrates powder XRD patterns of Example 1
(V.sub.2O.sub.5.sub._300), Example 2 (V.sub.2O.sub.5.sub._400),
Example 3 (V.sub.2O.sub.5.sub._SG_300), and Comparative Example 1
(V.sub.2O.sub.5.sub._500). FIG. 2 illustrates powder XRD patterns
of Example 3 (V.sub.2O.sub.5.sub._.sub.SG.sub._300), and Examples 4
to 9 and Comparative Examples 2 and 3 (xwt %
V.sub.2O.sub.5/TiO.sub.2). In the powder XRD patterns of Example 1
(V.sub.2O.sub.5.sub._300), Example 2 (V.sub.2O.sub.5.sub._400),
Example 3 (V.sub.2O.sub.5.sub._.sub.SG.sub._300), and Comparative
Example 1 (V.sub.2O.sub.5.sub._500), only peaks for V.sub.2O.sub.5
were observed regardless of the thermal decomposition temperature
and the production method. In the powder XRD patterns of Examples 4
to 9 and Comparative Examples 2 and 3 (xwt %
V.sub.2O.sub.5/TiO.sub.2), peaks for V.sub.2O.sub.5 were not
observed at 9 wt % or less and thus V.sub.2O.sub.5 is believed to
be highly dispersed in TiO.sub.2. When the amount of V.sub.2O.sub.5
supported was increased to 20 wt %, peaks for V.sub.2O.sub.5 were
observed at 22.2.degree. and 27.4.degree., and the V.sub.2O.sub.5
peak intensity increased as the amount of V.sub.2O.sub.5 supported
was increased. On the other hand, the TiO.sub.2 peak intensity
tended to decrease.
1.2.2 Measurement of BET Specific Surface Area
(Measurement Method)
[0071] The BET specific surface area was measured with a
MicrotracBEL BELSORP-max. Pretreatment was performed in an Ar
atmosphere at 200.degree. C. for 2 hours, and then measurement was
performed at 196.degree. C.
[0072] (Measurement Result)
TABLE-US-00001 TABLE 1 BET specific surface area of vanadium
pentoxide catalyst BET specific Sample surface area/m.sup.2g.sup.-1
Example1 (V.sub.2O.sub.5--300) 16.6 Example2 (V.sub.2O.sub.5--400)
13.5 Comparative Example1 (V.sub.2O.sub.5--500) 4.68 Example3
(V.sub.2O.sub.5--SG_300) 62.9 Comparative Example2 (0.3 wt %
V.sub.2O.sub.5/TiO.sub.2) 62.8 Comparative Example3 (0.9 wt %
V.sub.2O.sub.5/TiO.sub.2) 59 Example4 (3.3 wt %
V.sub.2O.sub.5/TiO.sub.2) 55.4 Example5 (9 wt %
V.sub.2O.sub.5/TiO.sub.2) 54.6 Example6 (20 wt %
V.sub.2O.sub.5/TiO.sub.2) 48.3 Example7 (33 wt %
V.sub.2O.sub.5/TiO.sub.2) 41.2 Example8 (43 wt %
V.sub.2O.sub.5/TiO.sub.2) 49.4 Example9 (80 wt %
V.sub.2O.sub.5/TiO.sub.2) 34 Comparative Example4 (Existing
catalyst) 61.8
[0073] Table 1 shows BET specific surface areas of Example 1
(V.sub.2O.sub.5.sub._500), Example 2 (V.sub.2O.sub.5.sub._400),
Comparative Example 1 (V.sub.2O.sub.5.sub._500), Example 3
(V.sub.2O.sub.5.sub._.sub.SG.sub._300), Comparative Examples 2 and
3 and Examples 4 to 9 (xwt % V.sub.2O.sub.5/TiO.sub.2 catalyst),
and Comparative Example 4 (existing catalyst). In the vanadium
pentoxide catalysts obtained by thermally decomposing ammonium
vanadate, the BET specific surface area decreased with increasing
the thermal decomposition temperature. That is, the vanadium
pentoxide in Example 1 (V.sub.2O.sub.5.sub._500) in which the
thermal decomposition was performed at 300.degree. C. had a maximum
BET specific surface area of 16.6 m.sup.2 g.sup.-1. The vanadium
pentoxide obtained at 300.degree. C. through a sol-gel process had
a larger BET specific surface area of 62.9 m.sup.2 g.sup.-1. In
Examples 4 to 9 and Comparative Examples 2 and 3 (xwt %
V.sub.2O.sub.5/TiO.sub.2), as the amount of vanadium pentoxide
supported was increased, pores in TiO.sub.2 were filled and the BET
specific surface area decreased.
1.2.3 Measurement of Catalytic Activity
(Measurement Method)
[0074] An NH.sub.3-SCR reaction was performed using a fixed-bed
flow reactor under the conditions listed in Table 2 below. Among
gases that had passed through the catalytic layer, NO, NH.sub.3,
NO.sub.2, and N.sub.2O were analyzed with a Jasco FT-IR-4700.
TABLE-US-00002 TABLE 2 NH.sub.3-SCR measurement conditions Amount
of catalyst 0.375 mg Gas flow rate 250 mLmin.sup.-1 (NO: 250 ppm,
NH.sub.3: 250 ppm, O.sub.2: 4 vol %) (2000 ppm NO/Ar 31.3 mL
min.sup.-1) (2000 ppm NH.sub.3/Ar 31.3 mL min.sup.-1) (O.sub.2 14
mL min.sup.-1) (Ar 177.4 mL min.sup.-1) Space velocity 40,000
mLh.sup.-1g.sub.cat.sup.-1
[0075] Furthermore, the NO conversion ratio and the N.sub.2
selectivity were calculated from formulae below. Herein, NO.sub.in
represents a NO concentration at an inlet of a reaction tube,
NO.sub.out represents a NO concentration at an outlet of the
reaction tube, N.sub.2out represents a N.sub.2 concentration at the
outlet of the reaction tube, NH.sub.3in represents a NH.sub.3
concentration at the inlet of the reaction tube, and NH.sub.3out
represents a NH.sub.3 concentration at the outlet of the reaction
tube.
NO CONVERSION RATIO = NO in - NO out NO in .times. 100 [ Formula .
1 ] NO SELECTIVITY ( % ) = 2 * N 2 out ( NO in + NH 3 in ) - ( NO
out + NH 3 out ) .times. 100 ( 2 * N 2 out = ( NO in + NH 3 in ) -
( NO out + NH 3 out + NO 2 out + 2 * N 2 O out ) ) [ Formula . 2 ]
##EQU00001##
[0076] (Measurement Result)
[0077] FIG. 3 illustrates the NH.sub.3-SCR activity of the vanadium
pentoxide catalysts. In the case of the catalysts obtained by
thermally decomposing ammonium vanadate, the NO conversion ratio
increased as the thermal decomposition temperature was decreased.
The highest activity was exhibited in Example 1
(V.sub.2O.sub.5.sub._300.degree. C.) in which the catalyst was
obtained at a thermal decomposition temperature of 300.degree. C.
At a reaction temperature of 200.degree. C., a NO conversion ratio
of 80% or more was achieved when any of the catalysts in Example 1
(V.sub.2O.sub.5.sub._300.degree. C.), Example 2
(V.sub.2O.sub.5.sub._400.degree. C.), and Example 3
(V.sub.2O.sub.5.sub._SG_300.degree. C.) was used. Furthermore, the
NO conversion ratio was higher in any of Examples than in
Comparative Example 1 and Comparative Example 4.
[0078] The specific surface area of the vanadium pentoxide
increases as the thermal decomposition temperature is decreased.
Therefore, it is believed that the low-temperature NH.sub.3-SCR
activity that uses a bulk vanadium pentoxide catalyst is
attributable to the BET specific surface area. Hence, as described
above, the vanadium pentoxide was produced through a sol-gel
process that uses oxalic acid in order to increase the BET specific
surface area in Example 3. The BET specific surface area of the
vanadium pentoxide produced through this process is 62.9 m.sup.2
g.sup.-1 as shown in Table 1, which is about four times larger than
the BET specific surface areas of the vanadium pentoxides produced
through a thermal decomposition process. The NO conversion ratio in
Example 3 (V.sub.2O.sub.5.sub._SG_300.degree. C.) was increased by
80% to 200% at 100.degree. C. to 150.degree. C. compared with the
vanadium pentoxides produced through a thermal decomposition
process.
[0079] The N.sub.2 selectivity was almost 100% at any temperature.
FIG. 4 illustrates, as examples, the N.sub.2 selectivities in
Example 1 (V.sub.2O.sub.5.sub._300.degree. C.) and Comparative
Example 1 (V.sub.2O.sub.5.sub._500.degree. C.).
[0080] (Space Velocity Dependency)
[0081] In the case where the catalyst in Example 1
(V.sub.2O.sub.5.sub._300.degree. C.) was used, the space velocity
(for gas treatment) dependency was measured by performing the
selective catalytic reduction reaction under the conditions listed
in Table 3 below. FIG. 5 illustrates the measurement results. FIG.
5(a) illustrates the NO conversion ratio at a reaction temperature
of 120.degree. C. FIG. 5(b) illustrates the NO conversion ratio at
a reaction temperature of 100.degree. C. The 80% NO detoxification
was about 15 Lh.sup.-1 g.sub.cat.sup.-1 at 120.degree. C. and about
11 Lh.sup.-1 g.sub.cat.sup.-1 at 100.degree. C. In an experiment in
which the space velocity was changed, the N.sub.2 selectivity was
almost 100%.
TABLE-US-00003 TABLE 3 NH.sub.3-SCR measurement conditions Reaction
temperature 120 or 100.degree. C. Amount of catalyst 0.375 g, 0.750
g, 1.5 g Total gas flow rate 250 mLmin.sup.-1 (NO: 250 ppm,
NH.sub.3: 250 ppm, O.sub.2: 4 vol %, Ar balance) Space velocity
10-40 Lh.sup.-1g.sub.cat.sup.-1 Gas flow time 0.5 h
[0082] (Reaction in Coexistence with Water)
[0083] An experiment of the NH.sub.3-SCR reaction was performed
using the catalyst in Example 1 (V.sub.2O.sub.5.sub._300.degree.
C.) under the conditions listed in Table 4 below at a reaction
temperature of 150.degree. C. at a space velocity of 20 Lh.sup.-1
g.sub.cat.sup.-1. FIG. 6 illustrates a change in the NO conversion
ratio over time in the experiment. As a result of addition of 2.3%
H.sub.2O 1.5 hours after the start of the reaction, the NO
conversion ratio decreased from 64% to 50%. The addition of
H.sub.2O did not change the N.sub.2 selectivity. The N.sub.2
selectivity was 100%. As a result of stop of the addition of water
3.5 hours after the start of the reaction, the NO conversion ratio
increased to 67%.
TABLE-US-00004 TABLE 4 NH.sub.3-SCR measurement conditions Reaction
temperature 150.degree. C. Amount of catalyst 0.375 g Total gas
flow rate 250 mLmin.sup.-1 (NO: 250 ppm, NH.sub.3: 250 ppm,
O.sub.2: 4 vol %, Ar balance) Space velocity 20
Lh.sup.-1g.sub.cat.sup.-1
[0084] (Reaction in Coexistence with S)
[0085] Under the same conditions as those of the experiment of the
reaction in coexistence with water, 100 ppm SO.sub.2 was caused to
flow through a reaction gas. FIG. 7 illustrates the experimental
results. No change occurred to the catalytic activity of NO. After
the completion of the temperature increase to 150.degree. C., the
SO.sub.2 concentration did not decrease though H.sub.2O and O.sub.2
were constantly present. Consequently, SO.sub.2 did not react.
Accordingly, the denitration catalysts in Examples were found to
have S resistance.
[0086] (Relationship Between Amount of Vanadium Pentoxide Supported
and NO Conversion Ratio)
[0087] FIG. 8 illustrates the relationship between the amount of
vanadium pentoxide supported and the NO conversion ratio at each
reaction temperature. FIG. 8(a) illustrates the relationship
between the amount of vanadium pentoxide supported and the NO
conversion ratio at a reaction temperature of 120.degree. C.
Similarly, FIG. 8(b) illustrates the relationship between the
amount of vanadium pentoxide supported and the NO conversion ratio
at a reaction temperature of 150.degree. C., and FIG. 8(c)
illustrates the relationship at a reaction temperature of
100.degree. C. In each of the graphs, the catalyst in which the
amount of vanadium pentoxide supported is 100 wt % is the
denitration catalyst V.sub.2O.sub.5.sub._.sub.SG.sub._300 produced
in Example 3. The points plotted using a square indicate a NO
conversion ratio of the existing catalyst in Comparative Example 4.
All the graphs showed that, on the whole, the NO conversion ratio
increased as the amount of vanadium pentoxide supported was
increased. Herein, all the graphs showed that the catalyst in which
the amount of vanadium pentoxide supported was 3.3 wt % had a
higher NO conversion ratio than the catalyst in which the amount of
vanadium pentoxide supported was 9.0 wt %. Specifically, as
illustrated in FIG. 8(a), in the NH.sub.3-SCR reaction at a
reaction temperature of 120.degree. C., the NO conversion ratio
reached 80% when the amount of vanadium pentoxide supported was
increased to 80 wt %. As illustrated in FIG. 8(b), in the
NH.sub.3-SCR reaction at a reaction temperature of 150.degree. C.,
the NO conversion ratio considerably increased when the amount of
vanadium pentoxide supported was increased to 3.3 wt %. As
illustrated in FIG. 8(c), in the selective catalytic reduction
reaction at a reaction temperature of 100.degree. C., the
denitration catalyst in which the amount of vanadium pentoxide
supported was 80 wt % had a considerably increased NO conversion
ratio compared with the denitration catalysts in which the amounts
of vanadium pentoxide supported were 43 wt % or less.
[0088] (Relationship Between BET Specific Surface Area and NO
Conversion Ratio)
[0089] FIG. 9(a) illustrates the relationship between the BET
specific surface area and the NO conversion ratio of the
denitration catalysts in which vanadium pentoxide was supported on
titanium oxide. In the denitration catalyst in which vanadium
pentoxide was supported on titanium oxide, as the amount of
vanadium pentoxide supported was increased, the BET specific
surface area decreased, but the activity increased on the whole.
FIG. 9(b) illustrates the relationship between the BET specific
surface area and the NO conversion ratio of both the denitration
catalysts in which vanadium pentoxide was supported on titanium
oxide and the denitration catalysts in which vanadium pentoxide was
not supported on titanium oxide. In the catalysts in which vanadium
pentoxide was not supported on titanium oxide, the activity
increased with increasing the BET specific surface area.
2. V.sub.2O.sub.5 Catalyst Produced Through Sol-Gel Process
2.1 Examples (Examples 10 to 14)
[0090] In "Example 3" of the above-described "1.1 Examples and
Comparative Examples", ammonium vanadate was dissolved in an oxalic
acid solution such that the molar ratio of vanadium and oxalic acid
was 1:3, then water was evaporated, drying was performed, and the
resulting dried powder was fired. Thus, a denitration catalyst was
produced. In the denitration catalysts of Examples 10 to 14, the
molar ratios of vanadium and oxalic acid were set to 1:1, 1:2, 1:3,
1:4, and 1:5, respectively. Specifically, as described above,
ammonium vanadate was dissolved in an oxalic acid solution (molar
ratio of vanadium:oxalic acid=1:1 to 1:5). After ammonium vanadate
was completely dissolved, water in the solution was evaporated on a
hot stirrer, and drying was performed in a dryer at 120.degree. C.
for one night. Then, the dried powder was fired in the air at
300.degree. C. for 4 hours. The sample names were given as
"V.sub.2O.sub.5SG_1:1" (Example 10), "V.sub.2O.sub.5.sub._SG_1:2"
(Example 11), "V.sub.2O.sub.5.sub._SG_1:3" (Example 12),
"V.sub.2O.sub.5.sub._SG_1:4" (Example 13), and
"V.sub.2O.sub.5.sub._SG_1:5" (Example 14). Herein, the
"V.sub.2O.sub.5.sub._.sub.SG.sub._300" in "Example 3" of "1.1
Examples and Comparative Examples" and "V.sub.2O.sub.5.sub._SG_1:3"
in Example 12 were substantially the same, but the sample name
"V.sub.2O.sub.5.sub._SG_1:3" in "Example 12" was used for the sake
of convenience of description. To increase the BET specific surface
area, a surfactant may be added to the oxalic acid solution.
Examples of the surfactant include anionic surfactants such as
hexadecyltrimethylammonium bromide (CTAB), sodium lauryl sulfate
(SDS), and hexadecylamine; cationic surfactants; amphoteric
surfactants; and nonionic surfactants.
2.2 Evaluation
2.2.1 Powder X-Ray Diffraction
(Diffraction Method)
[0091] In the same manner as in 1.2.1, powder X-ray diffraction
analysis was performed with a Rigaku smart lab using Cu-Ka.
[0092] (Diffraction Result)
[0093] FIG. 10 illustrates powder XRD patterns of Examples 10 to
(V.sub.2O.sub.5.sub._SG). In the vanadium pentoxides (Examples 10,
11, and 14) produced using the solutions having vanadium:oxalic
acid ratios of 1:1, 1:2, and 1:5, only peaks for orthorhombic
V.sub.2O.sub.5 were detected. In the vanadium pentoxides (Examples
12 and 13) produced using the solutions having vanadium:oxalic acid
ratios of 1:3 and 1:4, an unidentified peak was detected at
11.degree. in addition to the peaks for orthorhombic
V.sub.2O.sub.5. However, the peak has not been identified yet.
2.2.2 Measurement of BET Specific Surface Area
(Measurement Method)
[0094] In the same manner as in 1.2.3, the BET specific surface
area was measured with a MicrotracBEL BELSORP-max. Pretreatment was
performed in an Ar atmosphere at 200.degree. C. for 2 hours, and
then measurement was performed at 196.degree. C.
[0095] (Measurement Result)
TABLE-US-00005 TABLE 5 BET specific surface area of vanadium
pentoxide catalyst BET specific BET specific surface area before
surface area after Catalyst reaction/m.sup.2g.sup.-1
reaction/m.sup.2g.sup.-1 Example10 (V.sub.2O.sub.5--SG_1:1) 29.9
n.d. Example11 (V.sub.2O.sub.5--SG_1:2) 33.5 n.d. Example12
(V.sub.2O.sub.5--SG_1:3) 62.9 43.4 Example13
(V.sub.2O.sub.5--SG_1:4) 57.0 n.d. Example14
(V.sub.2O.sub.5--SG_1:5) n.d. n.d.
[0096] Table 5 shows BET specific surface areas of Example 10
(V.sub.2O.sub.5.sub._SG_1:1), Example 11
(V.sub.2O.sub.5.sub._SG_1:2), Example 12
(V.sub.2O.sub.5.sub._SG_1:3), Example 13
(V.sub.2O.sub.5.sub._SG_1:4), and Example 14
(V.sub.2O.sub.5.sub._SG_1:5). As the ratio of the oxalic acid was
increased, the specific surface area increased at vanadium:oxalic
acid ratios of 1:1 to 1:3. When the ratio of the oxalic acid was
further increased, the specific surface area decreased. The
specific surface area in Example 12 (V.sub.2O.sub.5.sub._SG_1:3)
after the catalytic activity test described below considerably
decreased to 43.4 m.sup.2 g.sup.-1 compared with the specific
surface area before the catalytic activity test.
2.2.3 Measurement of Catalytic Activity
(Measurement Method)
[0097] By the same measurement method as in 1.2.4, the NH.sub.3-SCR
activity of each V.sub.2O.sub.5.sub._SG catalyst was measured and
the NO conversion ratio was calculated.
[0098] (Measurement Result)
[0099] FIG. 11 illustrates the NH.sub.3-SCR activity of each
V.sub.2O.sub.5.sub._SG catalyst. FIG. 11(a) illustrates the NO
conversion ratio plotted against reaction temperature in the
NH.sub.3-SCR reaction that uses each catalyst. FIG. 11(b)
illustrates the relationship between the vanadium:oxalic acid ratio
and the NO conversion ratio at a reaction temperature of
120.degree. C. In the catalyst of Example 12
(V.sub.2O.sub.5.sub._SG_1:3) having a vanadium:oxalic acid ratio of
1:3, the highest NO conversion ratio was achieved. When the oxalic
acid was further added, the NO conversion ratio decreased. The NO
conversion ratio in Example 13 (V.sub.2O.sub.5.sub._SG_1:4) was
lower than that in Example 11 (V.sub.2O.sub.5.sub._SG_1:2) despite
the fact that the specific surface area in Example 13 was larger
than that in Example 11.
[0100] (Relationship Between Specific Surface Area and NO
Conversion Ratio)
[0101] FIG. 12 illustrates the relationship between the BET
specific surface area and the NO conversion ratio in Examples 10 to
13 (V.sub.2O.sub.5.sub._SG), Example 1 (V.sub.2O.sub.5.sub._500),
Example 2 (V.sub.2O.sub.5.sub._400), and Comparative Example 1
(V.sub.2O.sub.5.sub._500). The point plotted using a square
indicates the relationship between the BET specific surface area
and the NO conversion ratio after the selective catalytic reduction
reaction in Example 12 (V.sub.2O.sub.5.sub._SG_1:3). As described
above, it was shown that the highest NO conversion ratio was
achieved in the catalyst of Example 12 (V.sub.2O.sub.5.sub._SG_1:3)
having a vanadium:oxalic acid ratio of 1:3.
2.2.4 Characterization by NH.sub.3-TPD
(Measurement Method)
[0102] The amount of acid sites on the surface of the catalyst can
be estimated by NH.sub.3-TPD (TPD: temperature programed
desorption). In a BELCAT manufactured by MicrotracBEL Corp., 0.1 g
of each of the catalysts in Example 1 (V.sub.2O.sub.5.sub._500),
Example 2 (V.sub.2O.sub.5.sub._400), Comparative Example 1
(V.sub.2O.sub.5.sub._500), Example 11 (V.sub.2O.sub.5.sub._SG_1:2),
and Example 12 (V.sub.2O.sub.5.sub._SG_1:3) was pretreated at
300.degree. C. for 1 hour while He (50 ml/min) was caused to flow.
Then, the temperature was decreased to 100.degree. C., and 5%
ammonia/He (50 ml/min) was caused to flow for 30 minutes to adsorb
ammonia. The flow gas was changed to He (50 ml/min) and this state
was kept for 30 minutes for stabilization. Then, the temperature
was increased at 10.degree. C./min and ammonia, which has a mass
number of 16, was monitored with a mass spectrometer.
[0103] (Measurement Result)
TABLE-US-00006 TABLE 6 Measured amount of NH.sub.3 desorbed by
NH.sub.3-TPD Amount of NH.sub.3 Catalyst desorbed/mmolg.sup.-1
Example1 (V.sub.2O.sub.5--300) 22.9 Example2 (V.sub.2O.sub.5--400)
14.0 Comparative Example1 (V.sub.2O.sub.5--500) 5.21 Example11
(V.sub.2O.sub.5--SG_1:2) 51.4 Example12 (V.sub.2O.sub.5--SG_1:3)
77.5
[0104] Table 6 shows the measurement results of the amount of
NH.sub.3 desorbed when the catalysts in Example 1
(V.sub.2O.sub.5.sub._500), Example 2 (V.sub.2O.sub.5.sub._400),
Comparative Example 1 (V.sub.2O.sub.5.sub._500), Example 11
(V.sub.2O.sub.5.sub._SG_1:2), and Example 12
(V.sub.2O.sub.5.sub._SG_1:3) were used. FIG. 13 is a graph obtained
by plotting the amount of NH.sub.3 desorbed as a function of the
BET specific surface area of each catalyst. The graph in FIG. 13
showed that the amount of NH.sub.3 desorbed increased substantially
in proportion to the BET specific surface area of V.sub.2O.sub.5.
FIG. 14 is a graph obtained by plotting the NO conversion ratio as
a function of the amount of NH.sub.3 desorbed in each catalyst. The
graph showed that the NO conversion ratio increased as the catalyst
had a larger amount of NH.sub.3 desorbed, that is, a larger amount
of acid sites on the surface of the catalyst.
[0105] As described above, the denitration catalyst of the present
invention that contains 3.3 wt % or more of vanadium oxide in terms
of vanadium pentoxide and has a specific surface area of 10
m.sup.2/g or more exhibits a high denitration efficiency at a low
temperature of 200.degree. C. or lower in the selective catalytic
reduction reaction that uses ammonia as a reducing agent. On the
other hand, oxidation of SO.sub.2 is not found.
* * * * *