U.S. patent application number 09/928197 was filed with the patent office on 2002-05-30 for promoted multi-metal oxide catalyst.
Invention is credited to Chaturvedi, Sanjay, Gaffney, Anne Mae, Han, Scott, Heffner, Michele Doreen, Nhu Le, Dominique Hung, Song, Ruozhi, Vickery, Elsie Mae.
Application Number | 20020065431 09/928197 |
Document ID | / |
Family ID | 27540063 |
Filed Date | 2002-05-30 |
United States Patent
Application |
20020065431 |
Kind Code |
A1 |
Chaturvedi, Sanjay ; et
al. |
May 30, 2002 |
Promoted multi-metal oxide catalyst
Abstract
A catalyst comprising a promoted mixed metal oxide is useful for
the vapor phase oxidation of an alkane or a mixture of an alkane
and an alkene to an unsaturated carboxylic acid and for the vapor
phase ammoxidation of an alkane or a mixture of an alkane and an
alkene to an unsaturated nitrile.
Inventors: |
Chaturvedi, Sanjay;
(Horsham, PA) ; Gaffney, Anne Mae; (West Chester,
PA) ; Han, Scott; (Lawrenceville, NJ) ;
Heffner, Michele Doreen; (Chalfont, PA) ; Song,
Ruozhi; (Wilmington, DE) ; Nhu Le, Dominique
Hung; (Upper Darby, PA) ; Vickery, Elsie Mae;
(Jenkintown, PA) |
Correspondence
Address: |
ROHM AND HAAS COMPANY
PATENT DEPARTMENT
100 INDEPENDENCE MALL WEST
PHILADELPHIA
PA
19106-2399
US
|
Family ID: |
27540063 |
Appl. No.: |
09/928197 |
Filed: |
August 10, 2001 |
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60235979 |
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Current U.S.
Class: |
562/546 ;
502/254; 502/255; 562/547 |
Current CPC
Class: |
B01J 23/8877 20130101;
Y02P 20/52 20151101; C07C 253/24 20130101; B01J 2523/00 20130101;
B01J 23/20 20130101; C07C 51/215 20130101; B01J 27/0576 20130101;
B01J 23/686 20130101; C07C 51/252 20130101; B01J 37/08 20130101;
B01J 23/28 20130101; B01J 23/6525 20130101; B01J 23/002 20130101;
C07C 51/215 20130101; C07C 57/04 20130101; C07C 51/252 20130101;
C07C 57/04 20130101; C07C 253/24 20130101; C07C 255/08 20130101;
B01J 2523/00 20130101; B01J 2523/18 20130101; B01J 2523/55
20130101; B01J 2523/56 20130101; B01J 2523/64 20130101; B01J
2523/68 20130101; B01J 2523/00 20130101; B01J 2523/19 20130101;
B01J 2523/55 20130101; B01J 2523/56 20130101; B01J 2523/64
20130101; B01J 2523/68 20130101; B01J 2523/00 20130101; B01J
2523/55 20130101; B01J 2523/56 20130101; B01J 2523/64 20130101;
B01J 2523/68 20130101; B01J 2523/824 20130101; B01J 2523/00
20130101; B01J 2523/55 20130101; B01J 2523/56 20130101; B01J
2523/64 20130101; B01J 2523/68 20130101; B01J 2523/847 20130101;
B01J 2523/00 20130101; B01J 2523/17 20130101; B01J 2523/55
20130101; B01J 2523/56 20130101; B01J 2523/64 20130101; B01J
2523/68 20130101; B01J 2523/00 20130101; B01J 2523/55 20130101;
B01J 2523/56 20130101; B01J 2523/64 20130101; B01J 2523/68
20130101 |
Class at
Publication: |
562/546 ;
562/547; 502/254; 502/255 |
International
Class: |
C07C 051/16; B01J
021/12; B01J 021/14 |
Claims
What is claimed is:
1. A catalyst comprising a promoted mixed metal oxide having the
empirical formula A.sub.aM.sub.bN.sub.cX.sub.dZ.sub.eO.sub.fwherein
A is at least one element selected from the group consisting of Mo
and W, M is at least one element selected from the group consisting
of V and Ce, N is at least one element selected from the group
consisting of Te, Sb and Se, X is at least one element selected
from the group consisting of Nb, Ta, Ti, Al, Zr, Cr, Mn, Fe, Ru,
Co, Rh, Ni, Pt, Sb, Bi, B, In, As, Ge, Sn, Li, Na, K, Rb, Cs, Fr,
Be, Mg, Ca, Sr, Ba, Ra, Hf. Pb, P, Pm, Eu, Gd, Dy, Ho, Er, Tm, Yb
and Lu, and Z is selected from the group consisting of Ni, Pd, Cu,
Ag and Au; and wherein, when a=1, b=0.01 to 1.0, c=0.01 to 1.0,
d=0.01 to 1.0, e=0.001 to 0.1 and f is dependent on the oxidation
state of the other elements.
2. The catalyst according to claim 1, wherein M is V, N is Te
and/or Sb and X is Nb.
3. The catalyst according to claim 2, wherein A is Mo and N is
Te.
4. A process for producing an unsaturated carboxylic acid, which
comprises subjecting an alkane or a mixture of an alkane and an
alkene to a vapor phase catalytic oxidation reaction in the
presence of a catalyst containing a promoted mixed metal oxide
having the empirical formula
A.sub.aM.sub.bN.sub.cX.sub.dZ.sub.eO.sub.fwherein A is at least one
element selected from the group consisting of Mo and W, M is at
least one element selected from the group consisting of V and Ce, N
is at least one element selected from the group consisting of Te,
Sb and Se, X is at least one element selected from the group
consisting of Nb, Ta, Ti, Al, Zr, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt,
Sb, Bi, B, In, As, Ge, Sn, Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr,
Ba, Ra, Hf. Pb, P, Pm, Eu, Gd, Dy, Ho, Er, Tm, Yb and Lu, and Z is
selected from the group consisting of Ni, Pd, Cu, Ag and Au; and
wherein, when a=1, b=0.01 to 1.0, c=0.01 to 1.0, d=0.01 to 1.0,
e=0.001 to 0.1 and f is dependent on the oxidation state of the
other elements.
5. A process for producing an unsaturated nitrile, which comprises
subjecting an alkane, or a mixture of an alkane and an alkene, and
ammonia to a vapor phase catalytic oxidation reaction in the
presence of a catalyst containing a promoted mixed metal oxide
having the empirical formula
A.sub.aM.sub.bN.sub.cX.sub.dZ.sub.eO.sub.fwherein A is at least one
element selected from the group consisting of Mo and W, M is at
least one element selected from the group consisting of V and Ce, N
is at least one element selected from the group consisting of Te,
Sb and Se, X is at least one element selected from the group
consisting of Nb, Ta, Ti, Al, Zr, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt,
Sb, Bi, B, In, As, Ge, Sn, Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr,
Ba, Ra, Hf. Pb, P, Pm, Eu, Gd, Dy, Ho, Er, Tm, Yb and Lu, and Z is
selected from the group consisting of Ni, Pd, Cu, Ag and Au; and
wherein, when a=1, b=0.01 to 1.0, c=0.01 to 1.0, d=0.01 to 1.0,
e=0.001 to 1.0 and f is dependent on the oxidation state of the
other elements.
6. A catalyst produced by the process comprising: (1) admixing
compounds of the elements A, M, N, X and Z and at least one solvent
to form an admixture, wherein A is at least one element selected
from the group consisting of Mo and W, M is at least one element
selected from the group consisting of V and Ce, N is at least one
element selected from the group consisting of Te, Sb and Se, X is
at lest one element selected from the group consisting of Nb, Ta,
Ti, Al, Zr, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt, Bi, B, In, As, Ge, Sn,
Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Hf. Pb, P, Pm, Eu,
Gd, Dy, Ho, Er, Tm, Yb and Lu, and Z is selected from the group
consisting of Ni, Pd, Cu, Ag and Au and wherein the elements A, M,
N, X and Z are present in such amounts that the atomic ratio of
A:M:N:X:Z is 1:0.01 to 1.0:0.01 to 1.0:0.01 to 1.0:0.001 to 0.1;
(2) removing said at least one solvent from the admixture to obtain
a catalyst precursor; and (3) calcining said catalyst
precursor.
7. The catalyst according to claim 6, wherein at least one of the
compounds of the elements A, M, N, X and Z is an oxygen-containing
compound.
8. The catalyst according to claim 6, wherein the admixture is a
solution.
9. A process for producing an unsaturated carboxylic acid, which
comprises subjecting an alkane or a mixture of an alkane and an
alkene to a vapor phase catalytic oxidation reaction in the
presence of the catalyst according to claim 6.
10. A process for producing an unsaturated nitrile, which comprises
subjecting an alkane, or a mixture of an alkane and an alkene, and
ammonia to a vapor phase catalytic oxidation reaction in the
presence of the catalyst according to claim 6.
Description
[0001] The present invention relates to an improved catalyst for
the oxidation of alkanes or a mixture of alkanes and alkenes to
their corresponding unsaturated carboxylic acids by vapor phase
catalytic oxidation; to a method of making the catalyst; and to a
process for the vapor phase catalytic oxidation of alkanes or a
mixture of alkanes and alkenes to their corresponding unsaturated
carboxylic acids.
[0002] The present invention also relates to a method of producing
unsaturated nitrites by subjecting alkanes or a mixture of alkanes
and alkenes to vapor phase catalytic oxidation in the presence of
ammonia.
[0003] Nitriles, such as acrylonitrile and methacrylonitrile, have
been industrially produced as important intermediates for the
preparation of fibers, synthetic resins, synthetic rubbers, and the
like. The most popular method for producing such nitrites is to
subject an olefin such as propene or isobutene to a catalytic
reaction with ammonia and oxygen in the presence of a catalyst in a
gaseous phase at a high temperature. Known catalysts for conducting
this reaction include a Mo--Bi--P--O catalyst, a V--Sb--O catalyst,
an Sb--U--V--Ni--O catalyst, a Sb--Sn--O catalyst, a V--Sb--W--P--O
catalyst and a catalyst obtained by mechanically mixing a
V--Sb--W--O oxide and a Bi--Ce--Mo--W--O oxide. However, in view of
the price difference between propane and propene or between
isobutane and isobutene, attention has been drawn to the
development of a method for producing acrylonitrile or
methacrylonitrile by an ammoxidation reaction wherein a lower
alkane, such as propane or isobutane, is used as a starting
material, and it is catalytically reacted with ammonia and oxygen
in a gaseous phase in the presence of a catalyst.
[0004] In particular, U.S. Pat. No. 5,281,745 discloses a method
for producing an unsaturated nitrile comprising subjecting an
alkane and ammonia in the gaseous state to catalytic oxidation in
the presence of a catalyst which satisfies the conditions:
[0005] (1) the mixed metal oxide catalyst is represented by the
empirical formula
Mo.sub.aV.sub.bTe.sub.cX.sub.xO.sub.n
[0006] wherein X is at least one element selected from the group
consisting of niobium, tantalum, tungsten, titanium, aluminum,
zirconium, chromium, manganese, iron, ruthenium, cobalt, rhodium,
nickel, palladium, platinum, antimony, bismuth, boron and cerium
and, when a=1, b=0.01 to 1.0, c=0.01 to 1.0, x=0.01 to 1.0 and n is
a number such that the total valency of the metal elements is
satisfied; and
[0007] (2) the catalyst has X-ray diffraction peaks at the
following angles (.+-.0.3.degree.) of 2.theta. in its X-ray
diffraction pattern: 22.1.degree., 28.2.degree., 36.2.degree.,
45.2.degree. and 50.0.degree..
[0008] U.S. Pat. No. 5,231,214 discloses a method of nitrile
preparation comprising reacting an alkane in a gas phase contact
reaction with ammonia in the presence of a mixed metal oxide
catalyst of the formula
Mo.sub.aV.sub.bTe.sub.cNb.sub.dX.sub.xO.sub.n
[0009] wherein X represents one or more elements selected from
magnesium, calcium, strontium, barium, aluminum, gallium, thallium,
indium, tin, zirconium, hafnium, tantalum, chromium, manganese,
tungsten, iron, ruthenium, cobalt, rhodium, nickel, palladium,
zinc, lead, arsenic, antimony, bismuth, lanthanum and cerium and
when a=1, b=0.01 to 1.0, c=0.01 to 1.0, d=0 to 1.0, x=0.0005 to 1.0
and n is determined by the oxide form of the other elements.
[0010] Similarly, Japanese Laid-Open Patent Application Publication
No. 6-228073 discloses a method of nitrile preparation comprising
reacting an alkane in a gas phase contact reaction with ammonia in
the presence of a mixed metal oxide catalyst of the formula
W.sub.aV.sub.bTe.sub.cX.sub.xO.sub.n
[0011] wherein X represents one or more elements selected from
niobium, tantalum, titanium, aluminum, zirconium, chromium,
manganese, iron, ruthenium, cobalt, rhodium, nickel, palladium,
platinum, antimony, bismuth, indium and cerium and, when a=1,
b=0.01 to 1.0, c=0.01 to 1.0, x=0.01 to 1.0 and n is determined by
the oxide form of the elements.
[0012] U.S. Pat. No. 6,043,185 also discloses a catalyst useful in
the manufacture of acrylonitrile or methacrylonitrile by the
catalytic reaction in the vapor phase of a paraffin selected from
propane and isobutane with molecular oxygen and ammonia by
catalytic contact of the reactants in a reaction zone with a
catalyst, wherein the catalyst has the empirical formula
Mo.sub.aV.sub.bSb.sub.cGa.sub.dX.sub.eO.sub.x
[0013] where X is one or more of As, Te, Se, Nb, Ta, W, Ti, Zr, Cr,
Mn, Fe, Ru, Co, Rh, Ni, Pd, Pt, B, In, Ce, Re, Ir, Ge, Sn, Bi, Y,
Pr, an alkali metal and an alkaline earth metal; and when a=1,
b=0.0 to 0.99, c=0.01 to 0.9, d=0.01 to 0.5, e=0.0 to 1.0 and x is
determined by the oxidation state of the cations present.
[0014] Unsaturated carboxylic acids such as acrylic acid and
methacrylic acid are industrially important as starting materials
for various synthetic resins, coating materials and plasticizers.
Commercially, the current process for acrylic acid manufacture
involves a two-step catalytic oxidation reaction starting with a
propene feed. In the first stage, propene is converted to acrolein
over a modified bismuth molybdate catalyst. In the second stage,
acrolein product from the first stage is converted to acrylic acid
using a catalyst composed of mainly molybdenum and vanadium oxides.
In most cases, the catalyst formulations are proprietary to the
catalyst supplier, but, the technology is well established.
Moreover, there is an incentive to develop a single step process to
prepare the unsaturated acid from its corresponding alkene.
Therefore, the prior art describes cases where complex metal oxide
catalysts are utilized for the preparation of unsaturated acid from
a corresponding alkene in a single step.
[0015] European Published Patent Application No. 0 630 879 B1
discloses a process for producing an unsaturated aldehyde and a
carboxylic acid which comprises subjecting propene, isobutene or
tertiary butanol to gas phase catalytic oxidation with molecular
oxygen in the presence of (i) a catalyst composite oxide
represented by the formula
Mo.sub.aBi.sub.bFe.sub.cA.sub.dB.sub.eC.sub.fD.sub.gO.sub.x
[0016] wherein A represents Ni and/or Co, B represents at least one
element selected from Mn, Zn, Ca, Mg, Sn and Pb, C represents at
least one element selected from P, B, As, Te, W, Sb and Si, and D
represents at least one element selected from K, Rb, Cs and Tl; and
wherein, when a=12, 0<b.ltoreq.10, 0<c.ltoreq.10,
1.ltoreq.d.ltoreq.10, 0.ltoreq.e.ltoreq.10, 0.ltoreq.f.ltoreq.20
and 0.ltoreq.g.ltoreq.2, and x has a value dependent on the
oxidation state of the other elements; and (ii) a molybdenum oxide
which in itself is substantially inert to said gas phase catalytic
oxidation to provide the corresponding unsaturated aldehyde and
unsaturated carboxylic acid.
[0017] Japanese Laid-Open Patent Application Publication No.
07-053448 discloses the manufacture of acrylic acid by the
gas-phase catalytic oxidation of propene in the presence of mixed
metal oxides containing Mo, V, Te, O and X wherein X is at least
one of Nb, Ta, W, Ti, Al, Zr, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pd, Pt,
Sb, Bi, B, In, Li, Na, K, Rb, Cs and Ce.
[0018] Published International Application No. WO 00/09260
discloses a catalyst for selective oxidation of propene to acrylic
acid and acrolein containing a catalyst composition comprising the
elements Mo, V, La, Pd, Nb and X in the following ratio:
Mo.sub.aV.sub.bLa.sub.cPd.sub.dNb.sub.eX.sub.f
[0019] wherein X is Cu or Cr or a mixture thereof,
[0020] a is 1,
[0021] b is 0.01 to 0.9,
[0022] c is >0 to 0.2
[0023] d is 0.0000001 to 0.2,
[0024] e is 0 to 0.2, and
[0025] f is 0 to 0.2; and
[0026] wherein the numerical values of a, b, c, d, e and f
represent the relative gram-atom ratios of the elements Mo, V, La,
Pd, Nb and X, respectively, in the catalyst and the elements are
present in combination with oxygen.
[0027] Commercial incentives also exist for producing acrylic acid
using a lower cost propane feed. Therefore, the prior art describes
cases wherein a mixed metal oxide catalyst is used to convert
propane to acrylic acid in one step.
[0028] U.S. Pat. No. 5,380,933 discloses a method for producing an
unsaturated carboxylic acid comprising subjecting an alkane to a
vapor phase catalytic oxidation reaction in the presence of a
catalyst containing a mixed metal oxide comprising, as essential
components, Mo, V, Te, O and X, wherein X is at least one element
selected from the group consisting of niobium, tantalum, tungsten,
titanium, aluminum, zirconium, chromium, manganese, iron,
ruthenium, cobalt, rhodium, nickel, palladium, platinum, antimony,
bismuth, boron, indium and cerium; and wherein the proportions of
the respective essential components, based on the total amount of
the essential components, exclusive of oxygen, satisfy the
following relationships:
[0029] 0.25<r(Mo)<0.98, 0.003<r(V)<0.5,
0.003<r(Te)<0.5 and 0.003<r(X)<0.5, wherein r(Mo),
r(V), r(Te) and r(X) are the molar fractions of Mo, V, Te and X,
respectively, based on the total amount of the essential components
exclusive of oxygen.
[0030] Published International Application No. WO 00/29106
discloses a catalyst for selective oxidation of propane to
oxygenated products including acrylic acid, acrolein and acetic
acid, said catalyst system containing a catalyst composition
comprising
Mo.sub.aV.sub.bGa.sub.cPd.sub.dNb.sub.eX.sub.f
[0031] wherein X is at least one element selected from La, Te, Ge,
Zn, Si, In and W,
[0032] a is 1,
[0033] b is 0.01 to 0.9,
[0034] c is >0 to 0.2,
[0035] d is 0.0000001 to 0.2,
[0036] e is >0 to 0.2, and
[0037] f is 0.0 to 0.5; and
[0038] wherein the numerical values of a, b, c, d, e and f
represent the relative gram-atom ratios of the elements Mo, V, Ga,
Pd, Nb and X, respectively, in the catalyst and the elements are
present in combination with oxygen.
[0039] Japanese Laid-Open Patent Application Publication No.
2000-037623 discloses a method for producing an unsaturated
carboxylic acid comprising subjecting an alkane to a vapor phase
catalytic oxidation in the presence of a catalyst having the
empirical formula
MoV.sub.aNb.sub.bX.sub.cZ.sub.dO.sub.n
[0040] wherein X is at least one element selected from the group
consisting of Te and Sb, Z is at least one element selected from
the group consisting of W, Cr, Ta, Ti, Zr, Hf, Mn, Re, Fe, Ru, Co,
Rh, Ni, Pd, Pt, Ag, Zn, B, Al, Ga, In, Ge, Sn, Pb, P, Bi, Y, rare
earth elements and alkaline earth elements,
0.1.ltoreq.a.ltoreq.1.0, 0.01.ltoreq.b.ltoreq.1.0,
0.01.ltoreq.c.ltoreq.1.0, 0.ltoreq.d.ltoreq.1.0 and n is determined
by the oxidation states of the other elements.
[0041] Despite the above-noted attempts to provide new and improved
catalysts for the oxidation of alkanes to unsaturated carboxylic
acids and for the ammoxidation of alkanes to unsaturated nitriles,
one impediment to the provision of a commercially viable process
for such catalytic oxidations is the identification of a catalyst
providing adequate conversion and suitable selectivity, thereby
providing sufficient yield of the unsaturated product.
[0042] By the present invention, there are provided promoted
catalysts wherein the activity is greatly enhanced as to the base
catalyst and, hence, the overall yield of the desired reaction
product is also greatly enhanced.
[0043] Thus, in a first aspect, the present invention provides a
catalyst comprising a promoted mixed metal oxide having the
empirical formula
A.sub.aM.sub.bN.sub.cX.sub.dZ.sub.eO.sub.f
[0044] wherein A is at least one element selected from the group
consisting of Mo and W, M is at least one element selected from the
group consisting of V and Ce, N is at least one element selected
from the group consisting of Te, Sb and Se, X is at least one
element selected from the group consisting of Nb, Ta, Ti, Al, Zr,
Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt, Sb, Bi, B, In, As, Ge, Sn, Li, Na,
K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Hf, Pb, P, Pm, Eu, Gd, Dy,
Ho, Er, Tm, Yb and Lu, and Z is selected from the group consisting
of Ni, Pd, Cu, Ag and Au; and wherein, when a=1, b=0.01 to 1.0,
c=0.01 to 1.0, d=0.01 to 1.0, e=0.001 to 0.1 and f is dependent on
the oxidation state of the other elements.
[0045] In a second aspect, the present invention provides a process
for producing an unsaturated carboxylic acid, which comprises
subjecting an alkane or a mixture of an alkane and an alkene to a
vapor phase catalytic oxidation reaction in the presence of a
catalyst containing a promoted mixed metal oxide having the
empirical formula
A.sub.aM.sub.bN.sub.cX.sub.dZ.sub.eO.sub.f
[0046] wherein A is at least one element selected from the group
consisting of Mo and W, M is at least one element selected from the
group consisting of V and Ce, N is at least one element selected
from the group consisting of Te, Sb and Se, X is at least one
element selected from the group consisting of Nb, Ta, Ti, Al, Zr,
Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt, Sb, Bi, B, In, As, Ge, Sn, Li, Na,
K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Hf, Pb, P, Pm, Eu, Gd, Dy,
Ho, Er, Tm, Yb and Lu, and Z is selected from the group consisting
of Ni, Pd, Cu, Ag and Au; and wherein, when a=1, b=0.01 to 1.0,
c=0.01 to 1.0, d=0.01 to 1.0, e=0.001 to 0.1 and f is dependent on
the oxidation state of the other elements.
[0047] In a third aspect, the present invention provides a process
for producing an unsaturated nitrile, which comprises subjecting an
alkane, or a mixture of an alkane and an alkene, and ammonia to a
vapor phase catalytic oxidation reaction in the presence of a
catalyst containing a promoted mixed metal oxide having the
empirical formula
A.sub.aM.sub.bN.sub.cX.sub.dZ.sub.eO.sub.f
[0048] wherein A is at least one element selected from the group
consisting of Mo and W, M is at least one element selected from the
group consisting of V and Ce, N is at least one element selected
from the group consisting of Te, Sb and Se, X is at least one
element selected from the group consisting of Nb, Ta, Ti, Al, Zr,
Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt, Sb, Bi, B, In, As, Ge, Sn, Li, Na,
K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Hf. Pb, P, Pm, Eu, Gd, Dy,
Ho, Er, Tm, Yb and Lu, and Z is selected from the group consisting
of Ni, Pd, Cu, Ag and Au; and wherein, when a=1, b=0.01 to 1.0,
c=0.01 to 1.0, d=0.01 to 1.0, e=0.001 to 0.1 and f is dependent on
the oxidation state of the other elements.
[0049] In a fourth aspect, the present invention provides a
catalyst produced by the process comprising:
[0050] (1) admixing compounds of the elements A, M, N, X and Z and
at least one solvent to form an admixture, wherein A is at least
one element selected from the group consisting of Mo and W, M is at
least one element selected from the group consisting of V and Ce, N
is at least one element selected from the group consisting of Te,
Sb and Se, X is at least one element selected from the group
consisting of Nb, Ta, Ti, Al, Zr, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt,
Bi, B, In, As, Ge, Sn, Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba,
Ra, Hf, Pb, P, Pm, Eu, Gd, Dy, Ho, Er, Tm, Yb and Lu, and Z is
selected from the group consisting of Ni, Pd, Cu, Ag and Au, and
wherein the elements A, M, N, X and Z are present in such amounts
that the atomic ratio of A:M:N:X:Z is
[0051] 1:0.01 to 1.0:0.01 to 1.0:0.01 to 1.0:0.001 to 0.1;
[0052] (2) removing said at least one solvent from the admixture to
obtain a catalyst precursor; and
[0053] (3) calcining said catalyst precursor.
[0054] In a fifth aspect, the present invention provides a process
for producing an unsaturated Is; carboxylic acid, which comprises
subjecting an alkane or a mixture of an alkane and an alkene to a
vapor phase catalytic oxidation reaction in the presence of the
catalyst produced by the process comprising:
[0055] (1) admixing compounds of the elements A, M, N, X and Z and
at least one solvent to form an admixture, wherein A is at least
one element selected from the group consisting of Mo and W, M is at
least one element selected from the group consisting of V and Ce, N
is at least one element selected from the group consisting of Te,
Sb and Se, X is at lest one element selected from the group
consisting of Nb, Ta, Ti, Al, Zr, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt,
Bi, B, In, As, Ge, Sn, Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba,
Ra, Hf, Pb, P, Pm, Eu, Gd, Dy, Ho, Er, Tm, Yb and Lu, and Z is
selected from the group consisting of Ni, Pd, Cu, Ag and Au, and
wherein the elements A, M, N, X and Z are present in such amounts
that the atomic ratio of A:M:N:X:Z is
[0056] 1:0.01 to 1.0:0.01 to 1.0:0.01 to 1.0:0.001 to 0.1;
[0057] (2) removing said at least one solvent from the admixture to
obtain a catalyst precursor; and
[0058] (3) calcining said catalyst precursor.
[0059] In a sixth aspect, the present invention provides a process
for producing an unsaturated nitrile, which comprises subjecting an
alkane, or a mixture of an alkane and an alkene, and ammonia to a
vapor phase catalytic oxidation reaction in the presence of the
catalyst produced by the process comprising:
[0060] (1) admixing compounds of the elements A, M, N, X and Z and
at least one solvent to form an admixture, wherein A is at least
one element selected from the group consisting of Mo and W, M is at
least one element selected from the group consisting of V and Ce, N
is at least one element selected from the group consisting of Te,
Sb and Se, X is at lest one element selected from the group
consisting of Nb, Ta, Ti, Al, Zr, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt,
Bi, B, In, As, Ge, Sn, Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba,
Ra, Hf, Pb, P, Pm, Eu, Gd, Dy, Ho, Er, Tm, Yb and Lu, and Z is
selected from the group consisting of Ni, Pd, Cu, Ag and Au, and
wherein the elements A, M, N, X and Z are present in such amounts
that the atomic ratio of A:M:N:X:Z is
[0061] 1:0.01 to 1.0:0.01 to 1.0:0.01 to 1.0:0.001 to 0.1;
[0062] (2) removing said at least one solvent from the admixture to
obtain a catalyst precursor; and
[0063] (3) calcining said catalyst precursor.
[0064] The promoted mixed metal oxide to be used as a catalyst
component of the present invention has the empirical formula
A.sub.aM.sub.bN.sub.cX.sub.dZ.sub.eO.sub.f
[0065] wherein A is at least one element selected from the group
consisting of Mo and W, M is at least one element selected from the
group consisting of V and Ce, N is at least one element selected
from the group consisting of Te, Sb and Se, X is at least one
element selected from the group consisting of Nb, Ta, Ti, Al, Zr,
Cr, Mn, Fe, Ru, Co, Rh, Ni, Pt, Sb, Bi, B, In, As, Ge, Sn, Li, Na,
K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Hf, Pb, P, Pm, Eu, Gd, Dy,
Ho, Er, Tm, Yb and Lu, and Z is selected from the group consisting
of Ni, Pd, Cu, Ag and Au; and wherein, when a=1, b=0.01 to 1.0,
c=0.01 to 1.0, d=0.01 to 1.0, e=0.001 to 0.1 and f is dependent on
the oxidation state of the other elements.
[0066] Preferably, when a=1, b=0.1 to 0.5, c=0.05 to 0.5, d=0.01 to
0.5 and e=0.002 to 0.04. More preferably, when a=1, b=0.15 to 0.45,
c=0.05 to 0.45, d=0.01 to 0.1 and e=0.002 to 0.01. The value of f,
i.e. the amount of oxygen present, is dependent on the oxidation
state of the other elements in the catalyst. However, f is
typically in the range of from 3 to 4.7.
[0067] Preferred promoted mixed metal oxides have the empirical
formulae Mo.sub.aV.sub.bTe.sub.cNb.sub.dZ.sub.eO.sub.f and
W.sub.aV.sub.bTe.sub.cN- b.sub.dZ.sub.eO.sub.f wherein Z, a, b, c,
d, e and f are as previously defined.
[0068] Further, as the promoted mixed metal oxide, one having a
certain specific crystal structure is preferred. Specifically,
preference is given to the one which exhibits the following five
main diffraction peaks at specific diffraction angles 2.theta. in
the X-ray diffraction pattern of the promoted mixed metal oxide (as
measured using Cu--K.alpha. radiation as the source):
1 X-ray lattice plane Diffraction angle 2.theta. Spacing medium
Relative (.+-.0.3.degree.) (.ANG.) intensity 22.1.degree. 4.02 100
28.2.degree. 3.16 20.about.150 36.2.degree. 2.48 5.about.60
45.2.degree. 2.00 2.about.40 50.0.degree. 1.82 2.about.40
[0069] The intensity of the X-ray diffraction peaks may vary upon
the measuring of each crystal. However, the intensity, relative to
the peak intensity at 22.1.degree. being 100, is usually within the
above ranges. Generally, the peak intensities at
2.theta.=22.1.degree. and 28.2.degree. are distinctly observed.
However, so long as the above five diffraction peaks are
observable, the basic crystal structure is the same even if other
peaks are observed in addition to the five diffraction peaks, and
such a structure is useful for the present invention.
[0070] The promoted mixed metal oxide can be prepared in the
following manner.
[0071] In a first step a slurry or solution may be formed by
admixing metal compounds, to preferably at least one of which
contains oxygen, and at least one solvent in appropriate amounts to
form the slurry or solution. Preferably, a solution is formed at
this stage of the catalyst preparation. Generally, the metal
compounds contain elements A, M, N, X, Z and O, as previously
defined.
[0072] Suitable solvents include water; alcohols including, but not
limited to, methanol, ethanol, propanol, and diols, etc.; as well
as other polar solvents known in the art. Generally, water is
preferred. The water is any water suitable for use in chemical
syntheses including, without limitation, distilled water and
de-ionized water. The amount of water present is preferably an
amount sufficient to keep the elements substantially in solution
long enough to avoid or minimize compositional and/or phase
segregation during the preparation steps. Accordingly, the amount
of water will vary according to the amounts and solubilities of the
materials combined. However, as stated above, the amount of water
is preferably sufficient to ensure an aqueous solution is formed,
and not a slurry, at the time of mixing.
[0073] For example, when a mixed metal oxide of the formula
Mo.sub.aV.sub.bTe.sub.cNb.sub.dAu.sub.eO.sub.f wherein the element
A is Mo, the element M is V, the element N is Te and the element X
is Nb, is to be prepared, an aqueous solution of niobium oxalate
may be added to an aqueous solution or slurry of ammonium
heptamolybdate, ammonium metavanadate, telluric acid and ammonium
tetrachloroaurate, so that the atomic ratio of the respective metal
elements would be in the prescribed proportions.
[0074] Once the aqueous slurry or solution (preferably a solution)
is formed, the water is removed by any suitable method, known in
the art, to form a catalyst precursor. Such methods include,
without limitation, vacuum drying, freeze drying, spray drying,
rotary evaporation and air drying. Vacuum drying is generally
performed at pressures ranging from 10 mmHg to 500 mmHg. Freeze
drying typically entails freezing the slurry or solution, using,
for instance, liquid nitrogen, and drying the frozen slurry or
solution under vacuum. Spray drying is generally performed under an
inert atmosphere such as nitrogen or argon, with an inlet
temperature ranging from 125.degree. C. to 200.degree. C. and an
outlet temperature ranging from 75.degree. C. to 150.degree. C.
Rotary evaporation is generally performed at a bath temperature of
from 25.degree. C. to 90.degree. C. and at a pressure of from 10
mmHg to 760 mmHg, preferably at a bath temperature of from
40.degree. to 90.degree. C. and at a pressure of from 10 mmHg to
350 mmHg, more preferably at a bath temperature of from 40.degree.
C. to 60.degree. C. and at a pressure of from 10 mmHg to 40 mmHg.
Air drying may be effected at temperatures ranging from 25.degree.
C. to 90.degree. C. Rotary evaporation or air drying are generally
preferred.
[0075] Once obtained, the catalyst precursor is calcined. The
calcination may be conducted in an oxygen-containing atmosphere or
in the substantial absence of oxygen, e.g., in an inert atmosphere
or in vacuo. The inert atmosphere may be any material which is
substantially inert, i.e., does not react or interact with, the
catalyst precursor. Suitable examples include, without limitation,
nitrogen, argon, xenon, helium or mixtures thereof. Preferably, the
inert atmosphere is argon or nitrogen. The inert atmosphere may
flow over the surface of the catalyst precursor or may not flow
thereover (a static environment). When the inert atmosphere does
flow over the surface of the catalyst precursor, the flow rate can
vary over a wide range, e.g., at a space velocity of from 1 to 500
hr.sup.-1.
[0076] The calcination is usually performed at a temperature of
from 350.degree. C. to 850.degree. C., preferably from 400.degree.
C. to 700.degree. C., more preferably from 500.degree. C. to
640.degree. C. The calcination is performed for an amount of time
suitable to form the aforementioned catalyst. Typically, the
calcination is performed for from 0.5 to 30 hours, preferably from
1 to 25 hours, more preferably for from 1 to 15 hours, to obtain
the desired promoted mixed metal oxide.
[0077] In a preferred mode of operation, the catalyst precursor is
calcined in two stages. In the first stage, the catalyst precursor
is calcined in an oxidizing environment (e.g. air) at a temperature
of from 200.degree. C. to 400.degree. C., preferably from
275.degree. C. to 325.degree. C. for from 15 minutes to 8 hours,
preferably for from 1 to 3 hours. In the second stage, the material
from the first stage is calcined in a non-oxidizing environment
(e.g., an inert atmosphere) at a temperature of from 500.degree. C.
to 750.degree. C., preferably for from 550.degree. C. to
650.degree. C., for 15 minutes to 8 hours, preferably for from 1 to
3 hours. Optionally, a reducing gas, such as, for example, ammonia
or hydrogen, may be added during the second stage calcination.
[0078] In a particularly preferred mode of operation, the catalyst
precursor in the first stage is placed in the desired oxidizing
atmosphere at room temperature and then raised to the first stage
calcination temperature and held there for the desired first stage
calcination time. The atmosphere is then replaced with the desired
non-oxidizing atmosphere for the second stage calcination, the
temperature is raised to the desired second stage calcination
temperature and held there for the desired second stage calcination
time.
[0079] Although any type of heating mechanism, e.g., a furnace, may
be utilized during the calcination, it is preferred to conduct the
calcination under a flow of the designated gaseous environment.
Therefore, it is advantageous to conduct the calcination in a bed
with continuous flow of the desired gas(es) through the bed of
solid catalyst precursor particles.
[0080] With calcination, a catalyst is formed having the formula
A.sub.aM.sub.bN.sub.cX.sub.dZ.sub.eO.sub.f wherein A, M, N, X, Z,
O, a, b, c, d, e and f are as previously defined.
[0081] The starting materials for the above promoted mixed metal
oxide are not limited to those described above. A wide range of
materials including, for example, oxides, nitrates, halides or
oxyhalides, alkoxides, acetylacetonates, and organometallic
compounds may be used. For example, ammonium heptamolybdate may be
utilized for the source of molybdenum in the catalyst. However,
compounds such as MoO.sub.3, MoO.sub.2, MoCl.sub.5, MoOCl.sub.4,
Mo(OC.sub.2H.sub.5).sub.5, molybdenum acetylacetonate,
phosphomolybdic acid and silicomolybdic acid may also be utilized
instead of ammonium heptamolybdate. Similarly, ammonium
metavanadate may be utilized for the source of vanadium in the
catalyst. However, compounds such as V.sub.2O.sub.5,
V.sub.2O.sub.3, VOCl.sub.3, VCl.sub.4, VO(OC.sub.2H.sub.5).sub.3,
vanadium acetylacetonate and vanadyl acetylacetonate may also be
utilized instead of ammonium metavanadate. The tellurium source may
include telluric acid, TeCl.sub.4, Te(OC.sub.2H.sub.5).sub.5,
Te(OCH(CH.sub.3).sub.2).sub.4 and TeO.sub.2. The niobium source may
include ammonium niobium oxalate, Nb.sub.2O, NbCl.sub.5, niobic
acid or Nb(OC.sub.2H.sub.5).sub.5 as well as the more conventional
niobium oxalate. The nickel source may include nickel(II) acetate
tetrahydrate, Ni(NO.sub.3).sub.2, nickel(II) oxalate, NiO,
Ni(OH).sub.2, NiCl.sub.2, NiBr.sub.2, nickel(II) acetylacetonate,
nickel(II) sulfate, NiS or nickel metal. The palladium source may
include Pd(NO.sub.3).sub.2, palladium(II) acetate, palladium
oxalate, PdO, Pd(OH).sub.2, PdCl.sub.2, palladium acetylacetonate
or palladium metal. The copper source may be copper acetate, copper
acetate monohydrate, copper acetate hydrate, copper
acetylacetonate, copper bromide, copper carbonate, copper chloride,
copper chloride dihydrate, copper fluoride, copper formate hydrate,
copper gluconate, copper hydroxide, copper iodide, copper
methoxide, copper nitrate, copper nitrate hydrate, copper oxide,
copper tartrate hydrate or a solution of copper in an aqueous
inorganic acid, e.g., nitric acid. The silver source may be silver
acetate, silver acetylacetonate, silver benzoate, silver bromide,
silver carbonate, silver chloride, silver citrate hydrate, silver
fluoride, silver iodide, silver lactate, silver nitrate, silver
nitrite, silver oxide, silver phosphate or a solution of silver in
an aqueous inorganic acid, e.g., nitric acid. The gold source may
be ammonium tetrachloroaurate, gold bromide, gold chloride, gold
cyanide, is gold hydroxide, gold iodide, gold oxide, gold
trichloride acid and gold sulfide.
[0082] A promoted mixed metal oxide, thus obtained, exhibits
excellent catalytic activities by itself. However, the promoted
mixed metal oxide can be converted to a catalyst having higher
activities by grinding.
[0083] There is no particular restriction as to the grinding
method, and conventional methods may be employed. As a dry grinding
method, a method of using a gas stream grinder may, for example, be
mentioned wherein coarse particles are permitted to collide with
one another in a high speed gas stream for grinding. The grinding
may be conducted not only mechanically but also by using a mortar
or the like in the case of a small scale operation.
[0084] As a wet grinding method wherein grinding is conducted in a
wet state by adding water or an organic solvent to the above mixed
metal oxide, a conventional method of using a rotary cylinder-type
medium mill or a medium-stirring type mill, may be mentioned. The
rotary cylinder-type medium mill is a wet mill of the type wherein
a container for the object to be ground is rotated, and it
includes, for example, a ball mill and a rod mill. The
medium-stirring type mill is a wet mill of the type wherein the
object to be ground, contained in a container is stirred by a
stirring apparatus, and it includes, for example, a rotary screw
type mill, and a rotary disc type mill.
[0085] The conditions for grinding may suitably be set to meet the
nature of the above-mentioned promoted mixed metal oxide, the
viscosity, the concentration, etc. of the solvent used in the case
of wet grinding, or the optimum conditions of the grinding
apparatus. However, it is preferred that grinding is conducted
until the average particle size of the ground catalyst precursor
would usually be at most 20 .mu.m, more preferably at most 5 .mu.m.
Improvement in the catalytic performance may occur due to such
grinding.
[0086] Further, in some cases, it is possible to further improve
the catalytic activities by further adding a solvent to the ground
catalyst precursor to form a solution or slurry, followed by drying
again. There is no particular restriction as to the concentration
of the solution or slurry, and it is usual to adjust the solution
or slurry so that the total amount of the starting material
compounds for the ground catalyst precursor is from 10 to 60 wt %.
Then, this solution or slurry is dried by a method such as spray
drying, freeze drying, evaporation to dryness or vacuum drying,
preferably by the spray drying method. Further, similar drying may
be conducted also in the case where wet grinding is conducted.
[0087] The oxide obtained by the above-mentioned method may be used
as a final catalyst, but it may further be subjected to heat
treatment usually at a temperature of from 200.degree. to
700.degree. C. for from 0.1 to 10 hours.
[0088] The promoted mixed metal oxide thus obtained may be used by
itself as a solid catalyst, but may be formed into a catalyst
together with a suitable carrier such as silica, all alumina,
titania, aluminosilicate, diatomaceous earth or zirconia. Further,
it may be molded into a suitable shape and particle size depending
upon the scale or system of the reactor.
[0089] Alternatively, the metal components of the presently
contemplated catalyst may be supported on materials such as
alumina, silica, silica-alumina, zirconia, titania, etc. by
conventional incipient wetness techniques. In one typical method,
solutions containing the metals are contacted with the dry support
such that the support is wetted; then, the resultant wetted
material is dried, for example, at a temperature from room
temperature to 200.degree. C. followed by calcination as described
above. In another method, metal solutions are contacted with the
support, typically in volume ratios of greater than 3:1 (metal
solution: support), and the solution agitated such that the metal
ions are ion-exchanged onto the support. The metal-containing
support is then dried and calcined as detailed above.
[0090] In its second aspect, the present invention provides a
process for producing an unsaturated carboxylic acid, which
comprises subjecting an alkane, or a mixture of an alkane and an
alkene, to a vapor phase catalytic oxidation reaction in the
presence of a catalyst containing the above promoted mixed metal
oxide, to produce an unsaturated carboxylic acid.
[0091] In the production of such an unsaturated carboxylic acid, it
is preferred to employ a starting material gas which contains
steam. In such a case, as a starting material gas to be supplied to
the reaction system, a gas mixture comprising a steam-containing
alkane, or a steam-containing mixture of alkane and alkene, and an
oxygen-containing gas, is usually used. However, the
steam-containing alkane, or the steam-containing mixture of alkane
and alkene, and the oxygen-containing gas may be alternately
supplied to the reaction system. The steam to be employed may be
present in the form of steam gas in the reaction system, and the
manner of its introduction is not particularly limited.
[0092] Further, as a diluting gas, an inert gas such as nitrogen,
argon or helium may be supplied. The molar ratio (alkane or mixture
of alkane and alkene):(oxygen):(diluting gas):(H.sub.2O) in the
starting material gas is preferably (1):(0.1 to 10):(0 to 20):(0.2
to 70), more preferably (1):(1 to 5.0):(0 to 10):(5 to 40).
[0093] When steam is supplied together with the alkane, or the
mixture of alkane and alkene, as starting material gas, the
selectivity for an unsaturated carboxylic acid is distinctly
improved, and the unsaturated carboxylic acid can be obtained from
the alkane, or mixture of alkane and alkene, in good yield simply
by contacting in one stage. However, the conventional technique
utilizes a diluting gas such as nitrogen, argon or helium for the
purpose of diluting the starting material. As such a diluting gas,
to adjust the space velocity, the oxygen partial pressure and the
steam partial pressure, an inert gas such as nitrogen, argon or
helium may be used together with the steam.
[0094] As the starting material alkane it is preferred to employ a
C.sub.3-8alkane, particularly propane, isobutane or n-butane; more
preferably, propane or isobutane; most preferably, propane.
According to the present invention, from such an alkane, an
unsaturated carboxylic acid such as an .alpha.,.beta.-unsaturated
carboxylic acid can be obtained in good yield. For example, when
propane or isobutane is used as the starting material alkane,
acrylic acid or methacrylic acid will be obtained, respectively, in
good yield.
[0095] In the present invention, as the starting material mixture
of alkane and alkene, it is preferred to employ a mixture of
C.sub.3-8alkane and C.sub.3-8alkene, particularly propane and
propene, isobutane and isobutene or n-butane and n-butene. As the
starting material mixture of alkane and alkene, propane and propene
or isobutane and isobutene are more preferred. Most preferred is a
mixture of propane and propene. According to the present invention,
from such a mixture of an alkane and an alkene, an unsaturated
carboxylic acid such as an .alpha.,.beta.-unsaturated carboxylic
acid can be obtained in good yield. For example, when propane and
propene or isobutane and isobutene are used as the starting
material mixture of alkane and alkene, acrylic acid or methacrylic
acid will be obtained, respectively, in good yield. Preferably, in
the mixture of alkane and alkene, the alkene is present in an
amount of at least 0.5% by weight, more preferably at least 1.0% by
weight to 95% by weight; most preferably, 3% by weight to 90% by
weight.
[0096] As an alternative, an alkanol, such as isobutanol, which
will dehydrate under the reaction conditions to form its
corresponding alkene, i.e. isobutene, may also be used as a feed to
the present process or in conjunction with the previously mentioned
feed streams.
[0097] The purity of the starting material alkane is not
particularly limited, and an alkane containing a lower alkane such
as methane or ethane, air or carbon dioxide, as impurities, may be
used without any particular problem. Further, the starting material
alkane may be a mixture of various alkanes. Similarly, the purity
of the starting material mixture of alkane and alkene is not
particularly limited, and a mixture of alkane and alkene containing
a lower alkene such as ethene, a lower alkane such as methane or
ethane, air or carbon dioxide, as impurities, may be used without
any particular problem. Further, the starting material mixture of
alkane and alkene may be a mixture of various alkanes and
alkenes.
[0098] There is no limitation on the source of the alkene. It may
be purchased, per se, or in admixture with an alkane and/or other
impurities. Alternatively, it can be obtained as a by-product of
alkane oxidation. Similarly, there is no limitation on the source
of the alkane. It may be purchased, per se, or in admixture with an
alkene and/or other impurities. Moreover, the alkane, regardless of
source, and the alkene, regardless of source, may be blended as
desired.
[0099] The detailed mechanism of the oxidation reaction of the
present invention is not clearly understood, but the oxidation
reaction is carried out by oxygen atoms present in the above
promoted mixed metal oxide or by molecular oxygen present in the
feed gas. To incorporate molecular oxygen into the feed gas, such
molecular oxygen may be pure oxygen gas. However, it is usually
more economical to use an oxygen-containing gas such as air, since
purity is not particularly required.
[0100] It is also possible to use only an alkane, or a mixture of
alkane and alkene, substantially in the absence of molecular oxygen
for the vapor phase catalytic reaction. In such a case, it is
preferred to adopt a method wherein a part of the catalyst is
appropriately withdrawn from the reaction zone from time to time,
then sent to an oxidation regenerator, regenerated and then
returned to the reaction zone for reuse. As the regeneration method
of the catalyst, a method may, for example, be mentioned which
comprises contacting an oxidative gas such as oxygen, air or
nitrogen monoxide with the catalyst in the regenerator usually at a
temperature of from 300.degree. to 600.degree. C.
[0101] The second aspect of the present invention will be described
in further detail with respect to a case where propane is used as
the starting material alkane and air is used as the oxygen source.
The reaction system may be a fixed bed system or a fluidized bed
system. However, since the reaction is an exothermic reaction, a
fluidized bed system may preferably be employed whereby it is easy
to control the reaction temperature. The proportion of air to be
supplied to the reaction system is important for the selectivity
for the resulting acrylic acid, and it is usually at most 25 moles,
preferably from 0.2 to 18 moles per mole of propane, whereby high
selectivity for acrylic acid can be obtained. This reaction can be
conducted usually under atmospheric pressure, but may be conducted
under a slightly elevated pressure or slightly reduced pressure.
With respect to other alkanes such as isobutane, or to mixtures of
alkanes and alkenes such as propane and propene, the composition of
the feed gas may be selected in accordance with the conditions for
propane.
[0102] Typical reaction conditions for the oxidation of propane or
isobutane to acrylic acid or methacrylic acid may be utilized in
the practice of the present invention. The process may be practiced
in a single pass mode (only fresh feed is fed to the reactor) or in
a recycle mode (at least a portion of the reactor effluent is
returned to the reactor). General conditions for the process of the
present invention are as follows: the reaction temperature can vary
from 200.degree. C. to 700.degree. C., but is usually in the range
of from 200.degree. C. to 550.degree. C., more preferably
250.degree. C. to 480.degree. C., most preferably 300.degree. C. to
400.degree. C.; the gas space velocity, SV, in the vapor phase
reaction is usually within a range of from 100 to 10,000 hr.sup.-1,
preferably 300 to 6,000 hr.sup.-1, more preferably 300 to 2,000
hr.sup.-1; the average contact time with the catalyst can be from
0.01 to 10 seconds or more, but is usually in the range of from 0.1
to 10 seconds, preferably from 2 to 6 seconds; the pressure in the
reaction zone usually ranges from 0 to 75 psig, but is preferably
no more than 50 psig. In a single pass mode process, it is
preferred that the oxygen be supplied from an oxygen-containing gas
such as air. The single pass mode process may also be practiced
with oxygen addition. In the practice of the recycle mode process,
oxygen gas by itself is the preferred source so as to avoid the
build up of inert gases in the reaction zone.
[0103] Of course, in the oxidation reaction of the present
invention, it is important that the hydrocarbon and oxygen
concentrations in the feed gases be maintained at the appropriate
levels to minimize or avoid entering a flammable regime within the
reaction zone or especially at the outlet of the reactor zone.
Generally, it is preferred that the outlet oxygen levels be low to
both minimize after-burning and, particularly, in the recycle mode
of operation, to minimize the amount of oxygen in the recycled
gaseous effluent stream. In addition, operation of the reaction at
a low temperature (below 450.degree. C.) is extremely attractive
because after-burning becomes less of a problem which enables the
attainment of higher selectivity to the desired products. The
catalyst of the present invention operates more efficiently at the
lower temperature range set forth above, significantly reducing the
formation of acetic acid and carbon oxides, and increasing
selectivity to acrylic acid. As a diluting gas to adjust the space
velocity and the oxygen partial pressure, an inert gas such as
nitrogen, argon or helium may be employed.
[0104] When the oxidation reaction of propane, and especially the
oxidation reaction of propane and propene, is conducted by the
method of the present invention, carbon monoxide, carbon dioxide,
acetic acid, etc. may be produced as by-products, in addition to
acrylic acid. Further, in the method of the present invention, an
unsaturated aldehyde may sometimes be formed depending upon the
reaction conditions. For example, when propane is present in the
starting material mixture, acrolein may be formed; and when
isobutane is present in the starting material mixture, methacrolein
may be formed. In such a case, such an unsaturated aldehyde can be
converted to the desired unsaturated carboxylic acid by subjecting
it again to the vapor phase catalytic oxidation with the promoted
mixed metal oxide-containing catalyst of the present invention or
by subjecting it to a vapor phase catalytic oxidation reaction with
a conventional oxidation reaction catalyst for an unsaturated
aldehyde.
[0105] In its third aspect, the method of the present invention
comprises subjecting an alkane, or a mixture of an alkane and an
alkene, to a vapor phase catalytic oxidation reaction with ammonia
in the presence of a catalyst containing the above mixed metal
oxide, to produce an unsaturated nitrile.
[0106] In the production of such an unsaturated nitrile, as the
starting material alkane, it is preferred to employ a
C.sub.3-8alkane such as propane, butane, isobutane, pentane, hexane
and heptane. However, in view of the industrial application of
nitrites to be produced, it is preferred to employ a lower alkane
having 3 or 4 carbon atoms, particularly propane and isobutane.
[0107] Similarly, as the starting material mixture of alkane and
alkene, it is preferred to employ a mixture of C.sub.3-8alkane and
C.sub.3-8alkene such as propane and propene, butane and butene,
isobutane and isobutene, pentane and pentene, hexane and hexene,
and heptane and heptene. However, in view of the industrial
application of nitrites to be produced, it is more preferred to
employ a mixture of a lower alkane having 3 or 4 carbon atoms and a
lower alkene having 3 or 4 carbon atoms, particularly propane and
propene or isobutane and isobutene. Preferably, in the mixture of
alkane and alkene, the alkene is present in an amount of at least
0.5% by weight, more preferably at least 1.0% by weight to 95% by
weight, most preferably 3% by weight to 90% by weight.
[0108] The purity of the starting material alkane is not
particularly limited, and an alkane containing a lower alkane such
as methane or ethane, air or carbon dioxide, as impurities, may be
used without any particular problem. Further, the starting material
alkane may be a mixture of various alkanes. Similarly, the purity
of the starting material mixture of alkane and alkene is not
particularly limited, and a mixture of alkane and alkene containing
a lower alkene such as ethene, a lower alkane such as methane or
ethane, air or carbon dioxide, as impurities, may be used without
any particular problem. Further, the starting material mixture of
alkane and alkene may be a mixture of various alkanes and
alkenes.
[0109] There is no limitation on the source of the alkene. It may
be purchased, per se, or in admixture with an alkane and/or other
impurities. Alternatively, it can be obtained as a by-product of
alkane oxidation. Similarly, there is no limitation on the source
of the alkane. It may be purchased, per se, or in admixture with an
alkene and/or other impurities. Moreover, the alkane, regardless of
source, and the alkene, regardless of source, may be blended as
desired.
[0110] The detailed mechanism of the ammoxidation reaction of this
aspect of the present invention is not clearly understood. However,
the oxidation reaction is conducted by the oxygen atoms present in
the above promoted mixed metal oxide or by the molecular oxygen in
the feed gas. When molecular oxygen is incorporated in the feed
gas, the oxygen may be pure oxygen gas. However, since high purity
is not required, it is usually economical to use an
oxygen-containing gas such as air.
[0111] As the feed gas, it is possible to use a gas mixture
comprising an alkane, or a mixture of an alkane and an alkene,
ammonia and an oxygen-containing gas, However, a gas mixture
comprising an alkane or a mixture of an alkane and an alkene and
ammonia, and an oxygen-containing gas may be supplied
alternately.
[0112] When the gas phase catalytic reaction is conducted using an
alkane, or a mixture of an alkane and an alkene, and ammonia
substantially free from molecular oxygen, as the feed gas, it is
advisable to employ a method wherein a part of the catalyst is
periodically withdrawn and sent to an oxidation regenerator for
regeneration, and the regenerated catalyst is returned to the
reaction zone. As a method for regenerating the catalyst, a method
may be mentioned wherein an oxidizing gas such as oxygen, air or
nitrogen monoxide is permitted to flow through the catalyst in the
regenerator usually at a temperature of from 300.degree. C. to
600.degree. C.
[0113] The third aspect of the present invention will be described
in further detail with respect to a case where propane is used as
the starting material alkane and air is used as the oxygen source.
The proportion of air to be supplied for the reaction is important
with respect to the selectivity for the resulting acrylonitrile.
Namely, high selectivity for acrylonitrile is obtained when air is
supplied within a range of at most 25 moles, particularly 1 to 15
moles, per mole of the propane. The proportion of ammonia to be
supplied for the reaction is preferably within a range of from 0.2
to 5 moles, particularly from 0.5 to 3 moles, per mole of propane.
This reaction may usually be conducted under atmospheric pressure,
but may be conducted under a slightly increased pressure or a
slightly reduced pressure. With respect to other alkanes such as
isobutane, or to mixtures of alkanes and alkenes such as propane
and propene, the composition of the feed gas may be selected in
accordance with the conditions for propane.
[0114] The process of the third aspect of the present invention may
be conducted at a temperature of, for example, from 250.degree. C.
to 480.degree. C. More preferably, the temperature is from
300.degree. C. to 400.degree. C. The gas space velocity, SV, in the
gas phase reaction is usually within the range of from 100 to
10,000 hr.sup.-1, preferably from 300 to 6,000 hr.sup.-1, more
preferably from 300 to 2,000 hr.sup.-1. As a diluent gas, for
adjusting the space velocity and the oxygen partial pressure, an
inert gas such as nitrogen, argon or helium can be employed. When
ammoxidation of propane is conducted by the method of the present
invention, in addition to acrylonitrile, carbon monoxide, carbon
dioxide, acetonitrile, hydrocyanic acid and acrolein may form as
by-products.
EXAMPLES
Comparative Example 1
[0115] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.125O.sub.x was prepared in
the following manner; In a flask containing 300.2 g of water, 68.05
g of ammonium heptamolybdate tetrahydrate (Aldrich Chemical
Company), 13.39 g of ammonium metavanadate(Alfa-Aesar) and 20.36 g
of telluric acid (Aldrich Chemical Company) were dissolved upon
heating to 70.degree. C. After cooling to 40.degree. C., 328.03 g
of an aqueous solution of niobium oxalate (Reference Metals
Company) containing 1.35 wt. % Nb and 7.53 g oxalic acid (Aldrich
chemical Company) was mixed therewith to obtain a solution. The
water of this solution was removed via a rotary evaporator at a
temperature of 50.degree. C. and a pressure of 28 mmHg to obtain
the precursor solid. The solid precursor was calcined in a quartz
tube. (The quartz tube was placed in an oven under an air
atmosphere, the oven was heated to 275.degree. C. and held there
for one hour; a flow of argon (100 cc/min) over the precursor
material was then begun and the oven was heated to 600.degree. C.
and held there for two hours.) The catalyst, thus obtained, was
pressed in a mold and then broken and sieved to 10-20 mesh
granules. 10 g of these granules were packed into a stainless steel
U-tube reactor (inside diameter: 1.1 cm) for the gas phase
oxidation of propane, at various reaction temperatures. The U-tube
reactor was placed in a molten salt bath and fed with a mixture of
propane, air and steam having a feed ratio of propane/air/steam of
1/10/3 and having a space velocity of 1200 hr.sup.-1. The effluent
of the reactor was condensed to separate a liquid phase and a gas
phase. The gas phase was analyzed by gas chromatography to
determine the propane conversion. The liquid phase was also
analyzed by gas chromatography for the yield of acrylic acid. The
results (along with residence time and reactor temperature) are
shown in Table 1.
2TABLE 1 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Comp. 3 375 48.4 59.7 28.9 Ex. 1 Comp. 3 380 52.8 56.9
30.1 Ex. 1 Comp. 3 385 58.2 51.9 30.2 Ex. 1 Comp. 3 390 60.6 47.4
28.7 Ex. 1
Example 1
[0116] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.125Ni.sub.0.005O.sub.x was
prepared in the following manner: 34.03 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 6.71 g of
ammonium metavanadate (Alfa-Aesar), 10.08 g of telluric acid
(Aldrich Chemical Company) and 0.29 g of
Ni(NO.sub.3).sub.2.6H.sub.2O (Alfa-Aesar) were dissolved in 150.2 g
water upon heating to 70.degree. C. After cooling to 40.degree. C.,
164.25 g of an aqueous solution of niobium oxalate (Reference
Metals Company) containing 1.35 wt. % Nb and 3.77 g oxalic acid
(Aldrich chemical Company) was mixed therewith to obtain a
solution. The water of this solution was removed via a rotary
evaporator at a temperature of 50.degree. C. and a pressure of 28
mmHg to obtain the precursor solid. The solid precursor was
calcined in a quartz tube. (The quartz tube was placed in an oven
under an air atmosphere, the oven was heated to 275.degree. C. and
held there for one hour; a flow of argon (100 cc/min) over the
precursor material was then begun and the oven was heated to
600.degree. C. and held there for two hours.) The catalyst, thus
obtained, was pressed in a mold and then broken and sieved to 10-20
mesh granules. 10 g of these granules were packed into a stainless
steel U-tube reactor (inside diameter: 1.1 cm) for the gas phase
oxidation of propane, at various reaction temperatures and/or
reactor residence times. The U-tube reactor was placed in a molten
salt bath and fed with a mixture of propane, air and steam having a
feed ratio of propane/air/steam of 1/10/3 and having a space
velocity of 1200 hr.sup.-1. The effluent of the reactor was
condensed to separate a liquid phase and a gas phase. The gas phase
was analyzed by gas chromatography to determine the propane
conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
2.
3TABLE 2 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Ex. 1 3 345 48.3 72.8 35.2 Ex. 1 3 350 54.3 76.9 41.8
Ex. 1 3 355 62.1 74.4 46.2 Ex. 1 3 360 70.7 53.1 37.5 Ex. 1 4.5 350
69.3 53.7 37.2 Ex. 1 6 340 65.4 57.7 37.7
Example 2
[0117] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.125Ni.sub.0.01O.sub.x was
prepared in the following manner: 34.03 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 6.70 g of
ammonium metavanadate (Alfa-Aesar), 10.09 g of telluric acid
(Aldrich Chemical Company) and 0.554 g of
Ni(NO.sub.3).sub.2.6H.sub.2O (Alfa-Aesar) were dissolved in 150.1 g
water upon heating to 70.degree. C. After cooling to 40.degree. C.,
164.17 g of an aqueous solution of niobium oxalate (Reference
Metals Company) containing 1.35 wt. % Nb and 3.77 g oxalic acid
(Aldrich chemical Company) was mixed therewith to obtain a
solution. The water of this solution was removed via a rotary
evaporator at a temperature of 50.degree. C. and a pressure of 28
mmHg to obtain the precursor solid. The solid precursor was
calcined in a quartz tube. (The quartz tube was placed in an oven
under an air atmosphere, the oven was heated to 275.degree. C. and
held there for one hour; a flow of argon (100 cc/min) over the
precursor material was then begun and the oven was heated to
600.degree. C. and held there for two hours.) The catalyst, thus
obtained, was pressed in a mold and then broken and sieved to 10-20
mesh granules. 10 g of these granules were packed into a stainless
steel U-tube reactor (inside diameter: 1.1 cm) for the gas phase
oxidation of propane, at various reaction temperatures and/or
residence times. The U-tube reactor was placed in a molten salt
bath and fed with a mixture of propane, air and steam having a feed
ratio of propane/air/steam of 1/10/3 and having a space velocity of
1200 hr.sup.-1. The effluent of the reactor was condensed to
separate a liquid phase and a gas phase. The gas phase was analyzed
by gas chromatography to determine the propane conversion. The
liquid phase was also analyzed by gas chromatography for the yield
of acrylic acid. The results (along with residence time and reactor
temperature) are shown in Table 3.
4TABLE 3 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Ex. 2 3 340 42.3 70.9 30.0 Ex. 2 3 348 49.1 72.7 35.6
Ex. 2 3 352 56.2 70.5 39.6 Ex. 2 3 357 61.2 66.5 40.7 Ex. 2 3 362
67.4 67.3 42.4 Ex. 2 4.5 350 68.3 63.2 43.0 Ex. 2 6 365 67.4 65.9
44.5
Example 3
[0118] The catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23N- b.sub.0.125Ni.sub.0.01O.sub.x used
in example 11 was pressed in a mold and then broken and sieved to
10-20 mesh granules. 10 g of these granules were packed into a
stainless steel U-tube reactor (inside diameter: 1.1 cm) for the
gas phase oxidation of propane, at various reaction temperatures
and/or reactor residence times. The U-tube reactor was placed in a
molten salt bath and fed with a mixture of propane, air and steam
having a feed ratio of propane/air/steam of 1/15/14 and having a
space velocity of 1200 hr.sup.-1. The effluent of the reactor was
condensed to separate a liquid phase and a gas phase. The gas phase
was analyzed by gas chromatography to determine the propane
conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
4.
5TABLE 4 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Ex. 3 4 340 55.5 71.7 39.8 Ex. 3 3 350 65.3 68.4 44.6
Ex. 3 3 360 71.2 67.2 46.5
Examples 4
[0119] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.125Ni.sub.0.04O.sub.x was
prepared in the following manner: 34.01 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 6.70 g of
ammonium metavanadate (Alfa-Aesar), 10.08 g of telluric acid
(Aldrich Chemical Company) and 2.226 g of
Ni(NO.sub.3).sub.2.6H.sub.2O (Alfa-Aesar) were dissolved in 150.1 g
I water upon heating to 70.degree. C. After cooling to 40.degree.
C., 164.03 g of an aqueous solution of niobium oxalate (Reference
Metals Company) 1.35 wt. % Nb and 3.81 g oxalic acid (Aldrich
chemical Company) was mixed therewith to obtain a solution. The
water of this solution was removed via a rotary evaporator at a
temperature of 50.degree. C. and a pressure of 28 mmHg to obtain
the precursor solid. The solid precursor was calcined in a quartz
tube. (The quartz tube was placed in an oven under an air
atmosphere, the oven was heated to 275.degree. C. and held there
for one hour; a flow of argon (100 cc/min) over the precursor
material was then begun and the oven was heated to 600.degree. C.
and held there for two hours.) The catalyst, thus obtained, was
pressed in a mold and then broken and sieved to 10-20 mesh
granules. 10 g of these granules were packed into a stainless steel
U-tube reactor (inside diameter: 1.1 cm) for the gas phase
oxidation of propane. The U-tube reactor was placed in a molten
salt bath and fed with a mixture of propane, air and steam having a
feed ratio of propane/air/steam of 1/10/3 and having a space
velocity of 1200 hr.sup.-1. The effluent of the reactor was
condensed to separate a liquid phase and a gas phase. The gas phase
was analyzed by gas chromatography to determine the propane
conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
5.
6TABLE 5 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Ex. 4 3 350 44.7 70.5 31.5 Ex. 4 3 365 64.6 62.1
40.1
Comparative Example 2
[0120] In a flask containing 390 g of water, 46.4 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 9.2 g of
ammonium metavanadate(Alfa-Aesar) and 13.9 g of telluric acid
(Aldrich Chemical Company) were dissolved upon heating to
80.degree. C. After cooling to 20.degree. C., 201.3 g of an aqueous
solution of niobium oxalate (Reference Metals Company) containing
10.44 mmole/g of niobium was mixed therewith to obtain a solution.
The water of this solution was removed via a rotary evaporator at a
temperature of 50.degree. C. and a pressure of 28 mmHg to obtain 73
g of a precursor solid. 25 g of the solid precursor were calcined
in a quartz tube. (The quartz tube was placed in an oven under an
air atmosphere, the oven was heated to 275.degree. C. and held
there for one hour; a flow of argon (100 cc/min) over the precursor
material was then begun and the oven was heated to 600.degree. C.
and held there for two hours.) The catalyst, thus obtained, was
pressed in a mold and then broken and sieved to 10-20 mesh
granules. 10 g of these granules were packed into a stainless steel
U-tube reactor (inside diameter: 1.1 cm) for the gas phase
oxidation of propane. The U-tube reactor was placed in a molten
salt bath and fed with a mixture of propane, air and steam having a
feed ratio of propane/air/steam of 1/15/14 and having a space
velocity of 1200 hr.sup.-1. The effluent of the reactor was
condensed to separate a liquid phase and a gas phase. The gas phase
was analyzed by gas chromatography to determine the propane
conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
6.
7TABLE 6 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Comp. 3 360 30 46 14 Ex. 2 Comp. 3 370 38 50 19 Ex. 2
Comp. 3 390 67 40 27 Ex. 2
Example 5
[0121] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.08Pd.sub.0.04O.sub.x was
prepared in the following manner: 13.47 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 2.68 g of
ammonium metavanadate (Alfa-Aesar), 4.03 g of telluric acid
(Aldrich Chemical Company) and 0.68 g of
Pd(NO.sub.3).sub.3.XH.sub.2O (Alfa-Aesar) were dissolved in water
upon heating to 80.degree. C. After cooling to 20.degree. C., 59.07
g of an aqueous solution of niobium oxalate (Reference Metals
Company) containing 10.33 mmole/g of niobium was mixed therewith to
obtain a solution. The water of this solution was removed via a
rotary evaporator at a temperature of 50.degree. C. and a pressure
of 28 mmHg to obtain 28 g of a precursor solid. This solid
precursor were calcined in a quartz tube. (The quartz tube was
placed in an oven under an air atmosphere, the oven was heated to
275.degree. C. and held there for one hour; a flow of argon (100
cc/min) over the precursor material was then begun and the oven was
heated to 600.degree. C. and held there for two hours.) The
catalyst, thus obtained, was pressed in a mold and then broken and
sieved to 10-20 mesh granules. 10 g of these granules were packed
into a stainless steel U-tube reactor (inside diameter: 1.1 cm) for
the gas phase oxidation of propane. The U-tube reactor was placed
in a molten salt bath and fed with a mixture of propane, air and
steam having a feed ratio of propane/air/steam of 1/15/14 and
having a space velocity of 1200 hr.sup.-1. The effluent of the
reactor was condensed to separate a liquid phase and a gas phase.
The gas phase was analyzed by gas chromatography to determine the
propane conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
7.
8TABLE 7 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Ex. 5 3 350 27 71 19 Ex. 5 3 370 40 66 27 Ex. 5 3 380
56 60 34 Ex. 5 3 400 65 34 22
Example 6
[0122] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.08Pd.sub.0.01O.sub.x was
prepared by mixing ammonium heptamolybdate tetrahydrate (Aldrich
Chemical Company), ammonium metavanadate (Alfa-Aesar), telluric
acid (Aldrich Chemical Company) and Pd(NO.sub.3).sub.3.XH.sub.2O
(Alfa-Aesar) in the appropriate ratios in water heated to
80.degree. C. After cooling to 20.degree. C., the right amount of
an aqueous solution of niobium oxalate (Reference Metals Company)
was mixed therewith to obtain a solution. The water of this
solution was removed via a rotary evaporator at a temperature of
50.degree. C. and a pressure of 28 mmHg to obtain the precursor
solid. This solid precursor were calcined in a quartz tube. (The
quartz tube was placed in an oven under an air atmosphere, the oven
was heated to 275.degree. C. and held there for one hour; a flow of
argon (100 cc/min) over the precursor material was then begun and
the oven was heated to 600.degree. C. and held there for two
hours.) The catalyst, thus obtained, was pressed in a mold and then
broken and sieved to 10-20 mesh granules. 10 g of these granules
were packed into a stainless steel U-tube reactor (inside diameter:
1.1 cm) for the gas phase oxidation of propane. The U-tube reactor
was placed in a molten salt bath and fed with a mixture of propane,
air and steam having a feed ratio of propane/air/steam of 1/15/14
and having a space velocity of 1200 hr.sup.-1. The effluent of the
reactor was condensed to separate a liquid phase and a gas phase.
The gas phase was analyzed by gas chromatography to determine the
propane conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
8.
9TABLE 8 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Ex. 6 3 368 44.7 64.3 28.7 Ex. 6 4.5 375 62.4 60.3 37.6
Ex. 6 6 375 66 52.5 34.7
Example 7
[0123] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.08O.sub.x was prepared in
the manner as described in Example 1. Approximately 0.5 g of the
granules were packed into a quartz tube reactor for the gas phase
oxidation of propane. The oxidation was conducted with a feed ratio
of propane/steam/air of 1/3/96. The effluent from the reactor was
analyzed by infra-red spectrometry (IR) to determine the propane
conversion and the yield of acrylic acid. The results (along with
residence time and reaction temperature) are shown in Table 9.
10TABLE 9 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Ex. 7 3 280 12.1 44.5 5.4 Ex. 7 3 330 33.2 41.6 13.8
Ex. 7 3 350 46.0 32.6 15.0 Ex. 7 3 370 59.3 20.9 12.4 Ex. 7 3 380
65.9 16.2 10.7
Example 8
[0124] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.08Pd.sub.0.04O.sub.x was
prepared in the manner as described in Example 4. Approximately 0.5
g of the granules were packed into a quartz tube reactor for the
gas phase oxidation of propane. The oxidation was conducted with a
feed ratio of propane/steam/air of 1/3/96. The effluent from the
reactor was analyzed by infra-red spectrometry (IR) to determine
the propane conversion and the yield of acrylic acid. The results
(along with residence time and reaction temperature) are shown in
Table 10.
11TABLE 10 Residence Temp- Propane Acrylic Acid Acrylic Acid Time
erature Conversion Selectivity Yield Catalyst (sec) (.degree. C.)
(%) (%) (%) Ex. 8 3 370 25 92 23 Ex. 8 3 380 30 83 25 Ex. 8 3 390
37 73 27 Ex. 8 3 400 43 60 26
Comparative Example 3
[0125] 100 mL of an aqueous solution containing ammonium
heptamolybdate tetrahydrate (1.0M Mo), ammonium metavanadate (0.3M
V) and telluric acid (0.23 Te), formed by dissolving the
corresponding salts in water at 70.degree. C., was added to a 1000
mL rotavap flask. Then 50 mL of an aqueous solution of niobium
oxalate (0.25M Nb) and oxalic acid (0.31M) were added thereto.
After removing the water via a rotary evaporator with a warm water
bath at 50.degree. C. and 28 mm/Hg, the solid materials were
further dried in a vacuum oven at 25.degree. C. overnight and then
calcined. (Calcination was effected by placing the solid materials
in an air atmosphere and then heating them to 275.degree. C. at
10.degree. C./min and holding them under the air atmosphere at
275.degree. C. for one hour; the atmosphere was then changed to
argon and the material was heated from 275.degree. C. to
600.degree. C. at 2.degree. C./min and the material was held under
the argon atmosphere at 600.degree. C. for two hours.) The final
catalyst had a nominal composition of
Mo.sub.1V.sub.0.3Te.sub.0.23Nb.sub.0.125O.sub.f. The catalyst, thus
obtained, was pressed in a mold and then broken and sieved to 10-20
mesh granules for reactor evaluation.
Example 9
[0126] 50 mL of an aqueous solution containing ammonium
heptamolybdate tetrahydrate (1.0M Mo), ammonium metavanadate (0.3M
V) and telluric acid (0.23 Te), formed by dissolving the
corresponding salts in water at 70.degree. C., was added to a 1000
mL rotavap flask. Then 25 mL of an aqueous solution of niobium
oxalate (0.25M Nb) and oxalic acid (0.31M) and 1.25 mL of an
aqueous solution of copper (II) nitrate hemipentahydrate (0.1M)
were added thereto. After removing the water via a rotary
evaporator with a warm water bath at 50.degree. C. and 28 mm/Hg,
the solid materials were further dried in a vacuum oven at
25.degree. C. overnight. This solid precursor were calcined by
placing the solid materials in an air atmosphere and then heating
them to 275.degree. C. at 10.degree. C./min and holding them under
the air atmosphere at 275.degree. C. for one hour; the atmosphere
was then changed to argon and the material was heated from
275.degree. C. to 600.degree. C. at 2.degree. C./min and the
material was held under the argon atmosphere at 600.degree. C. for
two hours. The final catalyst had a nominal composition of
CU.sub.0.0025Mo.sub.1V.sub.0.3Te.sub.0.23Nb0.125O.sub.f. The
catalyst, thus obtained, was pressed in a mold and then broken and
sieved to 10-20 mesh granules for reactor evaluation.
[0127] The catalysts of Comparative Example 3 and Example 9 were
evaluated in a 10 cm long Pyrex.RTM. tube reactor (internal
diameter: 3.9 mm). The catalyst bed (4 cm long) was positioned with
glass wool at approximately mid-length in the reactor and was
heated with an electric furnace. Mass flow controllers and meters
regulated the gas flow rate. The oxidation was conducted using a
feed gas stream of propane, steam and air, with a feed ratio of
propane:steam:air of 1:3:96. The reactor effluent was analyzed by
an FTIR. The results (along with reaction temperature and residence
time) are shown in Table 11.
12TABLE 11 Residence Propane Acrylic Acid Temperature Time
Conversion Yield Catalyst (.degree. C.) (sec) (%) (%) Comp. Ex. 3
390 3 41 17 Ex. 9 390 3 59 27
Comparative Example 4
[0128] 100 mL of an aqueous solution containing ammonium
heptamolybdate tetrahydrate (1.0M Mo), ammonium metavanadate (0.3M
V) and telluric acid (0.23 Te), formed by dissolving the
corresponding salts in water at 70.degree. C., was added to a 1000
mL rotavap flask. Then 50 mL of an aqueous solution of niobium
oxalate (0.25M Nb) and oxalic acid (0.31M) were added thereto.
After removing the water via a rotary evaporator with a warm water
bath at 50.degree. C. and 28 mm/Hg, the solid materials were
further dried in a vacuum oven at 25.degree. C. overnight and then
calcined. (Calcination was effected by placing the solid materials
in an air atmosphere and then heating them to 275.degree. C. at
10.degree. C./min and holding them under the air atmosphere at
275.degree. C. for one hour; the atmosphere was then changed to
argon and the material was heated from 275.degree. C. to
600.degree. C. at 2.degree. C./min and the material was held under
the argon atmosphere at 600.degree. C. for two hours.) The final
catalyst had a nominal composition of
Mo.sub.1V.sub.0.3Te.sub.0.23Nb.sub.0.125O.sub.f. The catalyst, thus
obtained, was pressed in a mold and then broken and sieved to 10-20
mesh granules for reactor evaluation.
Example 10
[0129] 50 mL of an aqueous solution containing ammonium
heptamolybdate tetrahydrate (1.0M Mo), ammonium metavanadate (0.3M
V) and telluric acid (0.23 Te), formed by dissolving the
corresponding salts in water at 70.degree. C., was added to a 1000
mL rotavap flask. Then 25 mL of an aqueous solution of niobium
oxalate (0.25M Nb) and oxalic acid (0.31M) and 1.25 mL of an
aqueous solution of silver nitrate (0.1M) were added thereto. After
removing the water via a rotary evaporator with a warm water bath
at 50.degree. C. and 28 mm/Hg, the solid materials were further
dried in a vacuum oven at 25.degree. C. overnight. This solid
precursor were calcined by placing the solid materials in an air
atmosphere and then heating them to 275.degree. C. at 10.degree.
C./min and holding them under the air atmosphere at 275.degree. C.
for one hour; the atmosphere was then changed to argon and the
material was heated from 275.degree. C. to 600.degree. C. at
2.degree. C./min and the material was held under the argon
atmosphere at 600.degree. C. for two hours. The final catalyst had
a nominal composition of Ag.sub.0.0025Mo.sub.1V.sub.0.-
3Te.sub.0.23Nb.sub.0.125O.sub.f. The catalyst, thus obtained, was
pressed in a mold and then broken and sieved to 10-20 mesh granules
for reactor evaluation.
[0130] The catalysts of Comparative Example 4 and Example 10 were
evaluated in a 10 cm long Pyrex.RTM. tube reactor (internal
diameter: 3.9 mm). The catalyst bed (4 cm long) was positioned with
glass wool at approximately mid-length in the reactor and was
heated with an electric furnace. Mass flow controllers and meters
regulated the gas flow rate. The oxidation was conducted using a
feed gas stream of propane, steam and air, with a feed ratio of
propane:steam:air of 1:3:96. The reactor effluent was analyzed by
an FTIR. The results (along with reaction temperature and residence
time) are shown in Table 12.
13TABLE 12 Residence Propane Acrylic Acid Temperature Time
Conversion Yield Catalyst (.degree. C.) (sec) (%) (%) Comp. Ex. 4
390 3 41 17 Ex. 10 390 3 45 26
Comparative Example 5
[0131] In a flask containing 390 g of water, 46.4 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 9.2 g of
ammonium metavanadate(Alfa-Aesar) and 13.9 g of telluric acid
(Aldrich Chemical Company) were dissolved upon heating to
80.degree. C. After cooling to 20.degree. C., 201.3 g of an aqueous
solution of niobium oxalate (Reference Metals Company) containing
10.44 mmole/g of niobium was mixed therewith to obtain a solution.
The water of this solution was removed via a rotary evaporator at a
temperature of 50.degree. C. and a pressure of 28 mmHg to obtain 73
g of a precursor solid. 25 g of the solid precursor were calcined
in a quartz tube. (The quartz tube was placed in an oven under an
air atmosphere, the oven was heated to 275.degree. C. and held
there for one hour; a flow of argon (100 cc/min) over the precursor
material was then begun and the oven was heated to 600.degree. C.
and held there for two hours.) The catalyst, thus obtained, was
pressed in a mold and then broken and sieved to 10-20 mesh
granules. Approximately 0.5 g of the granules were packed into a
quartz tube reactor for the gas phase oxidation of propane. The
oxidation was conducted with a feed ratio of propane/steam/air of
1/3/96. The effluent from the reactor was analyzed by infra-red
spectrometry (IR) to determine the propane conversion and the yield
of acrylic acid. The results (along with residence time and
reaction temperature) are shown in Table 13.
14TABLE 13 Acrylic Acrylic Residence Temper- Propane Acid Acid Time
ature Conversion Selectivity Yield Catalyst (sec) (.degree. C.) (%)
(%) (%) Comp. Ex. 5 3 280 12.1 44.5 5.4 Comp. Ex. 5 3 330 33.2 41.6
13.8 Comp. Ex. 5 3 350 46.0 32.6 15.0 Comp. Ex. 5 3 370 59.3 20.9
12.4 Comp. Ex. 5 3 380 65.9 16.2 10.7
Example 11
[0132] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.08Ag.sub.0.04O.sub.x was
prepared in the following manner: 13.58 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 2.70 g of
ammonium metavanadate (Alfa-Aesar), 4.06 g of telluric acid
(Aldrich Chemical Company) and 0.51 g of Ag(NO.sub.3).sub.3
(Alfa-Aesar) were dissolved in water upon heating to 80.degree. C.
After cooling to 20.degree. C., 59.56 g of an aqueous solution of
niobium oxalate (Reference Metals Company) containing 10.33 mmole/g
of niobium was mixed therewith to obtain a solution. The water of
this solution was removed via a rotary evaporator at a temperature
of 50.degree. C. and a pressure of 28 mmHg to obtain 28 g of a
precursor solid. This solid precursor were calcined in a quartz
tube. (The quartz tube was placed in an oven under an air
atmosphere, the oven was heated to 275.degree. C. and held there
for one hour; a flow of argon (100 cc/min) over the precursor
material was then begun and the oven was heated to 600.degree. C.
and held there for two hours.) The catalyst, thus obtained, was
pressed in a mold and then broken and sieved to 10-20 mesh
granules. Approximately 0.5 g of the granules were packed into a
quartz tube reactor for the gas phase oxidation of propane. The
oxidation was conducted with a feed ratio of propane/steam/air of
1/3/96. The effluent from the reactor was analyzed by infra-red
spectrometry (IR) to determine the propane conversion and the yield
of acrylic acid. The results (along with residence time and
reaction temperature) are shown in Table 14.
15TABLE 14 Acrylic Residence Temper- Propane Acid Acrylic Acid Time
ature Conversion Selectivity Yield Catalyst (sec) (.degree. C.) (%)
(%) (%) Ex. 11 3 323 3 100 3 Ex. 11 3 337 4 100 4 Ex. 11 3 349 7 71
5 Ex. 11 3 357 8 63 5 Ex. 11 3 371 11 64 7 Ex. 11 3 382 15 47 7 Ex.
11 3 392 19 42 8
Comparative Example 6
[0133] In a flask containing 215 g of water, 25.68 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 5.06 g of
ammonium metavanadate(Alfa-Aesar) and 7.68 g of telluric acid
(Aldrich Chemical Company) were dissolved upon heating to
70.degree. C. After cooling to 40.degree. C., 122.94 g of an
aqueous solution of niobium oxalate (H. C. Starck) containing 1.25%
Nb to which 2.84 g of oxalic acid (Aldrich Chemical Company) had
been added was mixed therewith to obtain a solution. The water of
this solution was removed via a rotary evaporator at a temperature
of 50.degree. C. and a pressure of 28 mmHg to obtain 46 g of a
precursor solid. 23 g of this catalyst precursor solid was calcined
in a quartz tube. (The quartz tube was placed in an oven with a 100
cc/min flow of air through the tube, the oven was then heated to
275.degree. C. at 10.degree. C./min and held there for one hour;
then using a 100 cc/min flow of argon through the tube, the oven
was heated to 600.degree. C. at 2.degree. C./min and held there for
two hours.) The catalyst, thus obtained, was pressed in a mold and
then broken and sieved to 10-20 mesh granules. 10 g of these
granules were packed into a stainless steel U-tube reactor (inside
diameter: 1.1 cm) for the gas phase oxidation of propane. The
U-tube reactor was placed in a molten salt bath and fed with a
mixture of propane, air and steam having a feed ratio of
propane/air/steam of 1/15/14 and having a space velocity of 1200
hr.sup.-1. The effluent of the reactor was condensed to separate a
liquid phase and a gas phase. The gas phase was analyzed by gas
chromatography to determine the propane conversion. The liquid
phase was also analyzed by gas chromatography for the yield of
acrylic acid. The results (along with residence time and reactor
temperature) are shown in Table 15.
Example 12
[0134] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.08Au.sub.0.01O.sub.x was
prepared in the following manner: 12.93 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 2.55 g of
ammonium metavanadate (Alfa-Aesar), 3.87 g of telluric acid
(Aldrich Chemical Company) and 0.26 g of ammonium tetrachloroaurate
(Alfa-Aesar) were dissolved in water upon heating to 70.degree. C.
After cooling to 40.degree. C., 67.37 g of an aqueous solution of
niobium oxalate (H. C. Starck) containing 1.25% Nb to which 1.43 g
of oxalic acid (Aldrich Chemical Company) had been added was mixed
therewith to obtain a solution. The water of this solution was
removed via a rotary evaporator at a temperature of 50.degree. C.
and a pressure of 28 mmHg to obtain 28 g of a precursor solid. This
catalyst precursor solid was calcined in a quartz tube. (The quartz
tube was placed in an oven with a 100 cc/min flow of air through
the tube, the furnace was then heated to 275.degree. C. at
10.degree. C./min and held there for one hour; then using a 100
cc/min flow of argon through the tube, the oven was heated to
600.degree. C. at 2.degree. C./min and held there for two hours.)
The catalyst, thus obtained, was pressed in a mold and then broken
and sieved to 10-20 mesh granules. 10 g of these granules were
packed into a stainless steel U-tube reactor (inside diameter: 1.1
cm) for the gas phase oxidation of propane. The U-tube reactor was
placed in a molten salt bath and fed with a mixture of propane, air
and steam having a feed ratio of propane/air/steam of 1/15/14 and
having a space velocity of 1200 hr.sup.-1. The effluent of the
reactor was condensed to separate a liquid phase and a gas phase.
The gas phase was analyzed by gas chromatography to determine the
propane conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
15.
Example 13
[0135] A catalyst of nominal composition
Mo.sub.1.0V.sub.0.3Te.sub.0.23Nb.- sub.0.08Au.sub.0.005O.sub.x was
prepared in the following manner: 12.93 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 2.55 g of
ammonium metavanadate (Alfa-Aesar), 3.87 g of telluric acid
(Aldrich Chemical Company) and 0.13 g of ammonium tetrachloroaurate
(Alfa-Aesar) were dissolved in water upon heating to 70.degree. C.
After cooling to 40.degree. C., 67.37 g of an aqueous solution of
niobium oxalate (H. C. Starck) containing 1.25% Nb to which 1.43 g
of oxalic acid (Aldrich Chemical Company) had been added was mixed
therewith to obtain a solution. The water of this solution was
removed via a rotary evaporator at a temperature of 50.degree. C.
and a pressure of 28 mmHg to obtain 28 g of a precursor solid. This
catalyst precursor solid was calcined in a quartz tube. (The quartz
tube was placed in an oven with a 100 cc/min flow of air through
the tube, the furnace was then heated to 275.degree. C. at
10.degree. C./min and held there for one hour; then using a 100
cc/min flow of argon through the tube, the oven was heated to
600.degree. C. at 2.degree. C./min and held there for two hours.)
The catalyst, thus obtained, was pressed in a mold and then broken
and sieved to 10-20 mesh granules. 10 g of these granules were
packed into a stainless steel U-tube reactor (inside diameter: 1.1
cm) for the gas phase oxidation of propane. The U-tube reactor was
placed in a molten salt bath and fed with a mixture of propane, air
and steam having a feed ratio of propane/air/steam of 1/15/14 and
having a space velocity of 1200 hr.sup.-1. The effluent of the
reactor was condensed to separate a liquid phase and a gas phase.
The gas phase was analyzed by gas chromatography to determine the
propane conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
15.
Example 14
[0136] A catalyst of nominal composition
M.sub.1.0V.sub.0.3Te.sub.0.23Nb.s- ub.0.08Au.sub.0.0025O.sub.x was
prepared in the following manner: 12.93 g of ammonium
heptamolybdate tetrahydrate (Aldrich Chemical Company), 2.55 g of
ammonium metavanadate (Alfa-Aesar), 3.87 g of telluric acid
(Aldrich Chemical Company) and 0.07 g of ammonium tetrachloroaurate
(Alfa-Aesar) were dissolved in water upon heating to 70.degree. C.
After cooling to 40.degree. C., 67.37 g of an aqueous solution of
niobium oxalate (H. C. Starck) containing 1.25% Nb to which 1.43 g
of oxalic acid (Aldrich Chemical Company) had been added was mixed
therewith to obtain a solution. The water of this solution was
removed via a rotary evaporator at a temperature of 50.degree. C.
and a pressure of 28 mmHg to obtain 28 g of a precursor solid. This
catalyst precursor solid was calcined in a quartz tube. (The quartz
tube was placed in an oven with a 100 cc/min flow of argon through
the tube, the furnace was then heated to 275.degree. C. at
10.degree. C./min and held there for one hour; then using a 100
cc/min flow of argon through the tube, the oven was heated to
600.degree. C. at 2.degree. C./min and held there for two hours.)
The catalyst, thus obtained, was pressed in a mold and then broken
and sieved to 10-20 mesh granules. 10 g of these granules were
packed into a stainless steel U-tube reactor (inside diameter: 1.1
cm) for the gas phase oxidation of propane. The U-tube reactor was
placed in a molten salt bath and fed with a mixture of propane, air
and steam having a feed ratio of propane/air/steam of 1/15/14 and
having a space velocity of 1200 hr.sup.-1. The effluent of the
reactor was condensed to separate a liquid phase and a gas phase.
The gas phase was analyzed by gas chromatography to determine the
propane conversion. The liquid phase was also analyzed by gas
chromatography for the yield of acrylic acid. The results (along
with residence time and reactor temperature) are shown in Table
15.
16TABLE 15 Residence Propane Acrylic Acid Time Temperature
Conversion Yield Catalyst (sec) (.degree. C.) (%) (%) Comp. Ex. 6 3
400 24 14 Ex. 12 3 400 45 21 Ex. 13 3 400 52 22 Ex. 14 3 400 47
21
* * * * *