U.S. patent application number 11/641271 was filed with the patent office on 2008-06-19 for direct epoxidation catalyst.
Invention is credited to Roger A. Grey, Jude T. Ruszkay.
Application Number | 20080146825 11/641271 |
Document ID | / |
Family ID | 39313021 |
Filed Date | 2008-06-19 |
United States Patent
Application |
20080146825 |
Kind Code |
A1 |
Ruszkay; Jude T. ; et
al. |
June 19, 2008 |
DIRECT EPOXIDATION CATALYST
Abstract
A catalyst comprising a noble metal supported on a diatomaceous
earth and a transition metal zeolite is disclosed. The catalyst is
used in an epoxidation process comprising reacting an olefin,
hydrogen, and oxygen. The diatomaceous earth is readily available
and may be used in a slurry process without further particle size
enlargement.
Inventors: |
Ruszkay; Jude T.;
(Coatesville, PA) ; Grey; Roger A.; (West Chester,
PA) |
Correspondence
Address: |
LyondellBasell Industries
3801 WEST CHESTER PIKE
NEWTOWN SQUARE
PA
19073
US
|
Family ID: |
39313021 |
Appl. No.: |
11/641271 |
Filed: |
December 19, 2006 |
Current U.S.
Class: |
549/523 ; 502/66;
502/69; 549/518 |
Current CPC
Class: |
B01J 23/66 20130101;
B01J 29/89 20130101; B01J 23/52 20130101; B01J 35/023 20130101;
B01J 35/0006 20130101; B01J 37/06 20130101; C07D 301/06 20130101;
B01J 21/08 20130101 |
Class at
Publication: |
549/523 ; 502/69;
502/66; 549/518 |
International
Class: |
B01J 29/06 20060101
B01J029/06; B01J 29/064 20060101 B01J029/064; C07D 301/06 20060101
C07D301/06 |
Claims
1. A catalyst comprising a noble metal supported on a diatomaceous
earth and a transition metal zeolite.
2. The catalyst of claim 1 wherein the transition metal zeolite is
a titanium zeolite.
3. The catalyst of claim 1 wherein the transition metal zeolite is
TS-1.
4. The catalyst of claim 1 wherein the noble metal is selected from
the group consisting of gold, silver, platinum, palladium, iridium,
ruthenium, osmium, and mixtures thereof.
5. The catalyst of claim 1 wherein the noble metal is palladium,
gold, or a palladium-gold mixture.
6. The catalyst of claim 1 wherein the diatomaceous earth has a
mass median diameter from 1 to 200 .mu.m.
7. The catalyst of claim 1 wherein the diatomaceous earth has a
mass median diameter from 10 to 100 .mu.m.
8. An epoxidation process comprising reacting an olefin, hydrogen,
and oxygen in the presence of the catalyst of claim 1.
9. The process of claim 8 wherein the transition metal zeolite is a
titanium zeolite.
10. The process of claim 8 wherein the transition metal zeolite is
TS-1.
11. The process of claim 8 wherein the noble metal is selected from
the group consisting of gold, silver, platinum, palladium, iridium,
ruthenium, osmium, and mixtures thereof.
12. The process of claim 8 wherein the noble metal is palladium,
gold, or a palladium-gold mixture.
13. The process of claim 8 wherein the diatomaceous earth has a
mass median diameter from 1 to 200 .mu.m.
14. The process of claim 8 wherein the diatomaceous earth has a
mass median diameter from 10 to 100 .mu.m.
15. The process of claim 8 performed in a slurry.
16. The process of claim 8 performed in a fixed bed.
17. The process of claim 8 performed in a continuous mode.
18. The process of claim 8 performed in the presence of a
solvent.
19. The process of claim 18 performed in the presence of a
buffer.
20. The process of claim 8 wherein the olefin is propylene.
Description
FIELD OF THE INVENTION
[0001] The invention relates to a catalyst comprising a noble metal
supported on a diatomaceous earth and a transition metal zeolite.
The catalyst is used to produce an epoxide by reacting an olefin,
hydrogen, and oxygen.
BACKGROUND OF THE INVENTION
[0002] Direct epoxidation of higher olefins (containing three or
more carbons) such as propylene with oxygen and hydrogen has been
the focus of recent efforts. For example, the reaction may be
performed in the presence of a catalyst comprising gold and a
titanium-containing support (see, e.g., U.S. Pat. Nos. 5,623,090,
6,362,349, and 6,646,142), or a catalyst containing palladium and a
titanium zeolite (see, e.g., JP 4-352771).
[0003] Mixed catalyst systems for olefin epoxidation with hydrogen
and oxygen have also been disclosed. For example, Example 13 of JP
4-352771 describes the use of a mixture of titanosilicate and
Pd-on-carbon for propylene epoxidation. U.S. Pat. No. 6,008,388
describes a catalyst comprising a noble metal and a titanium or
vanadium zeolite, but additionally teaches that the Pd can be
incorporated into a support before mixing with the zeolite. The
catalyst supports disclosed include silica, alumina, and activated
carbon. U.S. Pat. No. 6,498,259 discloses the epoxidation of an
olefin with hydrogen and oxygen in a solvent containing a buffer in
the presence of a catalyst mixture containing a titanium zeolite
and a noble metal catalyst.
[0004] In a slurry epoxidation process using the mixed catalyst
systems, liquid and/or gas product streams need to be separated
from the solid catalyst particles. Generally it is necessary to
make titanium zeolites and the supported noble metal catalyst into
large enough particles (e.g., >1 .mu.m) to make such separation
(e.g., filtration) practically viable.
SUMMARY OF THE INVENTION
[0005] The invention is a catalyst comprising a noble metal
supported on a diatomaceous earth and a transition metal zeolite.
The catalyst is used in an epoxidation process comprising reacting
an olefin, hydrogen, and oxygen. Diatomaceous earth is readily
available and can be easily separated from a liquid and/or gas
effluent.
DETAILED DESCRIPTION OF THE INVENTION
[0006] The invention is a catalyst comprising a transition metal
zeolite. Zeolites are microporous crystalline solids with
well-defined structures. Generally they contain one or more of Si,
Ge, Al, B, P, or the like, in addition to oxygen. Many zeolites
occur naturally as minerals and are extensively mined in many parts
of the world. Others are synthetic and are made commercially for
specific uses. Zeolites have the ability to act as catalysts for
chemical reactions which take place mostly within the internal
cavities of the zeolites. Transition metal zeolites are zeolites
comprising transition metals in framework. A transition metal is a
Group 3-12 element. The first row of them are from Sc to Zn.
Preferred transition metals are Ti, V, Mn, Fe, Co, Cr, Zr, Nb, Mo,
and W. More preferred are Ti, V, Mo, and W. Most preferred is
Ti.
[0007] Preferred titanium zeolites are titanium silicates
(titanosilicates). Preferably, they contain no element other than
titanium, silicon, and oxygen in the lattice framework (see R.
Szostak, "Non-aluminosilicate Molecular Sieves," in Molecular
Sieves: Principles of Synthesis and Identification (1989), Van
Nostrand Reinhold, pp. 205-82). Small amounts of impurities, e.g.,
boron, iron, aluminum, phosphorous, copper, and the like, and
mixtures thereof, may be present in the lattice. The amount of
impurities is preferably less than 0.5 wt. %, more preferably less
than 0.1 wt. %. Preferred titanium silicates will generally have a
composition corresponding to the following empirical formula:
xTiO.sub.2(1--x)SiO.sub.2, where x is between 0.0001 and 0.5000.
More preferably, the value of x is from 0.01 to 0.125. The molar
ratio of Si to Ti in the lattice framework of the zeolite is
advantageously from 9.5:1 to 99:1, most preferably from 9.5:1 to
60:1. Particularly preferred titanium zeolites are titanium
silicalites (see Catal. Rev.-Sci. Eng., 39(3) (1997) 209). Examples
of these include TS-1 (titanium silicalite-1, a titanium silicalite
having an MFI topology analogous to that of the ZSM-5
aluminosilicate), TS-2 (having an MEL topology analogous to that of
the ZSM-11 aluminosilicate), and TS-3 (as described in Belgian Pat.
No. 1,001,038). Titanium zeolites having framework structures
isomorphous to zeolite beta, mordenite, and ZSM-12 are also
suitable for use. The most preferred is TS-1.
[0008] The catalyst comprises a noble metal. Suitable noble metals
include gold, silver, platinum, palladium, iridium, ruthenium,
osmium, rhenium, rhodium, and mixtures thereof. Preferred noble
metals are Pd, Pt, Au, Re, Ag, and mixtures thereof. Palladium,
gold, and their mixtures are particularly desirable. Typically, the
amount of noble metal present in the catalyst will be in the range
of from 0.01 to 20 wt. %, preferably 0.1 to 5 wt. %.
[0009] The catalyst comprises a diatomaceous earth. Diatomaceous
earth, also known as kieselguhr, or diatomite, is a naturally
occurring, highly structured, fine hydrous silica powder made up of
the remains of planktonic algae. Many different types of
diatomaceous earth are available commercially. Diatomaceous earth
is used in many applications as the uniquely porous nature of each
particle gives diatomite high surface area, low bulk density, high
permeability, high water absorption, and low abrasion. Diatomaceous
earth filter aids are used to prevent blinding of filter elements
and are used to clarify liquids in brewing, water treatment, wine
making, sugar refining, fruit juice production, and in industrial
chemicals processing. Diatomaceous earth functional fillers are
used in paints, rubber, plastics, pharmaceuticals, toothpastes,
polishes, and chemicals where performance is improved by the unique
properties of diatomaceous earth. Diatomaceous earth can also be
used as catalyst support. See Kenneth R. Engh, "Diatomite,"
Kirk-Othmer Encyclopedia of Chemical Technology online edition,
2006. See also U.S. Pat. Nos. 4,297,241, 4,285,927, and
6,746,597
[0010] Diatomaceous earth gives many advantages as a catalyst or a
catalyst support. First, diatomaceous earth is easy to filter. When
a solid catalyst is used in a slurry reaction, it is usually
necessary to separate the catalyst from a liquid and/or gas
reaction effluent. In a continuous slurry reaction, a liquid and/or
gas effluent needs to be continuously withdrawn from the reactor.
In either case, the ease of filtration improves the operation.
Second, commercially available diatomaceous earth materials can be
used in slurry reactions without the need of particle enlargement.
For example, diatomaceous earth materials available from
EaglePicher Filtration & Minerals, Inc. have median particle
sizes of 10-80 .mu.m (Technical Data Sheet,
http://www.eaglepicher.com). In comparison, other catalyst supports
(e.g., silica, alumina, and titania) would generally need to be
processed (e.g., spray-dried) to obtain particles of such
sizes.
[0011] The noble metal is supported on the diatomaceous earth. The
manner in which the noble metal is incorporated in a diatomaceous
earth is not critical. For example, the noble metal may be
supported on the diatomaceous earth by impregnation, ion-exchange,
adsorption, precipitation, or the like.
[0012] There are no particular restrictions regarding the choice of
the noble metal compound or complex used as the source of the noble
metal. Suitable compounds include nitrates, sulfates, halides
(e.g., chlorides, bromides), carboxylates (e.g., acetate), and
amine or phosphine complexes of noble metals (e.g., palladium(II)
tetraammine bromide, tetrakis(triphenylphosphine)
palladium(0)).
[0013] Similarly, the oxidation state of the noble metal is not
critical. Palladium, for instance, may be in an oxidation state
anywhere from 0 to +4 or any combination of such oxidation states.
To achieve the desired oxidation state or combination of oxidation
states, the noble metal compound after being introduced on the
diatomaceous earth may be fully or partially pre-reduced.
Satisfactory catalytic performance can, however, be attained
without any pre-reduction.
[0014] The weight ratio of the transition metal zeolite to noble
metal is not particularly critical. However, a transition metal
zeolite to noble metal weight ratio of from 10:1 to 5000:1 (grams
of transition metal zeolite per gram of noble metal) is
preferred.
[0015] The catalyst may comprise a promoter. A promoter helps to
improve the catalyst performance (e.g., activity, selectivity, life
of the catalyst). Preferred promoters include lead, zinc, alkaline
earth metals, lanthanide metals, and the like. Lead is particularly
preferred. The promoter may be added on the transition metal
zeolite and/or the diatomaceous earth. Preferably it is added to
the diatomaceous earth. While the choice of compound used as the
promoter source is not critical, suitable compounds include metal
carboxylates. (e.g., acetate), halides (e.g., chlorides, bromides,
iodides), nitrates, sulfate, and the like. The typical amount of
promoter metal present in the catalyst will be in the range of from
about 0.001 to 5 weight percent, preferably 0.001 to 2 weight
percent relative to the catalyst.
[0016] When the catalyst is used in a slurry, the diatomaceous
earth has preferably a mass median particle size in the range of 1
to 200 .mu.m, more preferably in the range of 10 to 100 .mu.m. The
mass median particle diameter is the diameter that divides half of
the mass ("Particle Size Measurement," Kirk-Othmer Encyclopedia of
Chemical Technology online edition, 2006).
[0017] The invention also includes an epoxidation process
comprising reacting an olefin, hydrogen, and oxygen in the presence
of the catalyst of the invention.
[0018] An olefin is used in the process. Suitable olefins include
any olefin having at least one carbon-carbon double bond, and
generally from 2 to 60 carbon atoms. Preferably the olefin is an
acyclic alkene of from 2 to 30 carbon atoms; the process is
particularly suitable for epoxidizing C.sub.2-C.sub.6 olefins. More
than one double bond may be present in the olefin molecule, as in a
diene or triene. The olefin may be a hydrocarbon or may contain
functional groups such as halogen, carboxyl, hydroxyl, ether,
carbonyl, cyano, or nitro groups, or the like. In a particularly
preferred process, the olefin is propylene and the epoxide is
propylene oxide.
[0019] Oxygen and hydrogen are required. Although any sources of
oxygen and hydrogen are suitable, molecular oxygen and molecular
hydrogen are preferred. The molar ratio of hydrogen to oxygen can
usually be varied in the range of H.sub.2:O.sub.2=1:100 to 5:1 and
is especially favorable at 1:5 to 2:1. The molar ratio of oxygen to
olefin is usually 1:1 to 1:20, and preferably 1:1.5 to 1:10.
Relatively high oxygen to olefin molar ratios (e.g., 1:1 to 1:3)
may be advantageous for certain olefins.
[0020] In addition to the olefin, oxygen, and hydrogen, an inert
gas is preferably used in the process. Any desired inert gas can be
used. Suitable inert gases include nitrogen, helium, argon, and
carbon dioxide. Saturated hydrocarbons with 1-8, especially 1-6,
and preferably 1-4 carbon atoms, e.g., methane, ethane, propane,
and n-butane, are also suitable. Nitrogen and saturated
C.sub.1-C.sub.4 hydrocarbons are preferred inert gases. Mixtures of
inert gases can also be used. The molar ratio of olefin to gas is
usually in the range of 100:1 to 1:10 and especially 20:1 to
1:10.
[0021] The process may be performed in a continuous flow,
semi-batch, or batch mode. A continuous flow process is preferred.
The catalyst is preferably in a slurry or a fixed bed. For a
fixed-bed process, the catalyst is preferably formed into
extrudates, tablets, granules, and the like.
[0022] It is advantageous to work at a pressure of 1-200 bars. The
process is carried out at a temperature effective to achieve the
desired olefin epoxidation, preferably at temperatures in the range
of 0-200.degree. C., more preferably, 20-150.degree. C. Preferably,
at least a portion of the reaction mixture is a liquid under the
reaction conditions.
[0023] A reaction solvent is preferably used in the process.
Suitable reaction solvents are liquid under the reaction
conditions. They include, for example, oxygen-containing
hydrocarbons such as alcohols, aromatic and aliphatic solvents such
as toluene and hexane, nitriles such as acetonitrile, carbon
dioxide, and water. Suitable oxygenated solvents include alcohols,
ethers, esters, ketones, carbon dioxide, water, and the like, and
mixtures thereof. Preferred oxygenated solvents include water and
lower aliphatic C.sub.1-C.sub.4 alcohols such as methanol, ethanol,
isopropanol, tert-butanol, and mixtures thereof. Fluorinated
alcohols can be used.
[0024] Where a reaction solvent is used, it may be advantageous to
use a buffer. The buffer is employed in the reaction to inhibit the
formation of glycols or glycol ethers during the epoxidation, and
it can improve the reaction rate and selectivities. The buffer is
typically added to the solvent to form a buffer solution, or the
solvent and the buffer are added separately. Useful buffers include
any suitable salts of oxyacids, the nature and proportions of which
in the mixture are such that the pH of their solutions preferably
ranges from 3 to 12, more preferably from 4 to 10, and most
preferably from 5 to 9. Suitable salts of oxyacids contain an anion
and a cation. The anion may include phosphate, carbonate,
bicarbonate, sulfate, carboxylates (e.g., acetate), borate,
hydroxide, silicate, aluminosilicate, or the like. The cation may
include ammonium, alkylammonium (e.g., tetraalkylammoniums,
pyridiniums), alkylphosphonium, alkali metal, and alkaline earth
metal ions, or the like. Examples include NH.sub.4, NBu.sub.4,
NMe.sub.4, Li, Na, K, Cs, Mg, and Ca cations. The preferred buffer
comprises an anion selected from the group consisting of phosphate,
carbonate, bicarbonate, sulfate, hydroxide, and acetate; and a
cation selected from the group consisting of ammonium,
alkylammonium, alkylphosphonium, alkali metal, and alkaline earth
metal ions. Buffers may preferably contain a combination of more
than one suitable salt. Typically, the concentration of the buffer
in the solvent is from 0.0001 M to 1 M, preferably from 0.0005 M to
0.3 M. The buffer may include ammonium hydroxide which can be
formed by adding ammonia gas to the reaction system. For instance,
one may use a pH=12-14 solution of ammonium hydroxide to balance
the pH of the reaction system. More preferred buffers include
alkali metal phosphates, ammonium phosphate, and ammonium
hydroxide. The ammonium phosphate buffer is particularly
preferred.
[0025] Following examples merely illustrate the invention. Those
skilled in the art will recognize many variations that are within
the spirit of the invention and scope of the claims.
EXAMPLE 1
Pd--Au ON FN-1, Calcined 300.degree. C.
Catalyst A
[0026] Diatomaceous earth FN-1 (EaglePicher Filtration and
Minerals, Inc., 30 g) is added to a solution made from deionized
water (120 g), aqueous sodium tetrachloroaurate solution (20.74 wt.
% gold, 0.795 g), and disodium tetrachloropalladate (from Aldrich
Chemical, 0.825 g). Sodium bicarbonate powder is added to the
slurry until the pH reaches 7.24. The slurry is allowed to react
for 4 h at 50.degree. C., then filtered. The solid is washed with
deionized water (7.times.80 g). The solid is then calcined in air
at 110.degree. C. for 4 h (10.degree. C./min from room temperature
to 110.degree. C.) and at 300.degree. C. for 4 h (2.degree. C./min
from 110.degree. C. to 300.degree. C.). The calcined solid is then
transferred to a quartz tube and treated with a gas containing 4
vol. % hydrogen in nitrogen at 100.degree. C. for 1 h (flow rate
100 mL/h) and then purged with nitrogen for 1 h. The final solid
(Catalyst A) contains 1.0 wt. % palladium and 0.44 wt. % gold.
EXAMPLE 2
Pd--Au ON FN-1, Calcined 550.degree. C.
Catalyst B
[0027] The procedure of Example 1 is repeated except that the solid
is calcined at 550.degree. C. before hydrogen reduction. The solid
obtained (Catalyst B) contains 1.0 wt. % palladium and 0.44 wt. %
gold.
EXAMPLE 3
Pd--Au on FN-1, Calcined 650.degree. C.
Catalyst C
[0028] The procedure of Example 1 is repeated except that the solid
is calcined at 650.degree. C. before hydrogen reduction. The solid
obtained (Catalyst C) contains 1.0 wt. % palladium and 0.44 wt. %
gold.
EXAMPLE 4
Pd--Au on FP-3, Calcined 300.degree. C.
Catalyst D
[0029] The procedure of Example 1 is repeated except that
diatomaceous earth FP-3 (EaglePicher Filtration and Minerals, Inc.,
30 g) is used instead of FN-1. The solid obtained (Catalyst D)
contains 0.75 wt. % palladium and 0.35 wt. % gold.
EXAMPLE 5
Pd--Au on FP-3, Calcined 550.degree. C.
Catalyst E
[0030] The procedure of Example 4 is repeated except that the solid
is calcined at 550.degree. C. before hydrogen reduction. The solid
obtained (Catalyst E) contains 0.75 wt. % palladium and 0.35 wt. %
gold.
EXAMPLE 6
Pd--Au on FW-14, Calcined 300.degree. C.
Catalyst F
[0031] The procedure of Example 1 is repeated except that
diatomaceous earth FW-14 (EaglePicher Filtration and Minerals,
Inc., 30 g) is used instead of FN-1. The solid obtained (Catalyst
F) contains 0.81 wt. % palladium and 0.33 wt. % gold.
Comparative example 7. Pd--Au on Titania
Catalyst G
[0032] A spray-dried anatase (average diameter 35 .mu.m, air
calcined at 700.degree. C. for 4 h, surface area 40 m.sup.2/g, 20
g) is added to a solution made from deionized water (80 g), an
aqueous sodium tetrachloroaurate solution (20.74 wt. % gold, 0.53
g), and disodium tetrachloropalladate (19.75 wt. % Pd, 1.01 g).
Sodium bicarbonate powder is added to the slurry until the pH
reaches 7.24. The slurry is allowed to react for 4 h at 50.degree.
C., then filtered. The solid is washed with deionized water
(7.times.80 g). The solid is then calcined in air at 110.degree. C.
for 4 h (at a rate of 10.degree. C./min from room temperature to
110.degree. C.) and at 550.degree. C. for 4 h (at a rate of
2.degree. C./min from 110.degree. C. to 550.degree. C.). The
calcined solid is transferred to a quartz tube and treated with a
gas containing 4 vol. % hydrogen in nitrogen at 100.degree. C. for
1 h (flow rate 100 mL/h) and then purged with nitrogen for 1 h. The
final solid (Catalyst G) contains 1.0 wt. % palladium and 0.42 wt.
% gold.
EXAMPLE 8
Propylene Epoxidation with Catalyst a
[0033] Titanium silicalite-1 (TS-1) is prepared by following
procedures disclosed in U.S. Pat. Nos. 4,410,501 and 4,833,260, and
calcined in air at 550.degree. C.
[0034] An ammonium phosphate buffer solution (0.1 M, pH 6) is
prepared as follows. Ammonium dihydrogen phosphate (11.5 g) is
dissolved in deionized water (900 g). Aqueous ammonium hydroxide
(30 wt. % NH.sub.4OH) is added to the solution until the pH reads 6
via a pH meter. The volume of the solution is then increased to
exactly 1000 mL with additional deionized water.
[0035] A 300-mL stainless steel reactor is charged with Catalyst A
(0.07 g), TS-1 powder (0.63 g), the buffer solution prepared above
(13 g), and methanol (100 g). The reactor is then charged to 300
psig with a feed gas consisting of 2 volume percent (vol. %)
hydrogen, 4 vol. % oxygen, 5 vol. % propylene, 0.5 vol. % methane,
and the balance nitrogen. The pressure in the reactor is maintained
at 300 psig via a back pressure regulator with the feed gases pass
continuously through the reactor at 1600 mL/min (measured at
23.degree. C. and 1 atmosphere pressure). In order to maintain a
constant solvent level in the reactor during the run, the oxygen,
nitrogen and propylene feeds are passed through a 2-L stainless
steel vessel (saturator) preceding the reactor containing 1.5 L of
methanol. The reaction mixture is heated to 60.degree. C. while it
is stirred at 1500 rpm. The gaseous effluent is analyzed by an
online gas chromatograph (GC) every hour. The liquid is analyzed by
offline GC at the end of the 18 h run. The products formed include
propylene oxide (PO), propane, and derivatives of propylene oxide
such as propylene glycol, propylene glycol monomethyl ethers,
dipropylene glycol, and dipropylene glycol methyl ethers. The
calculated results are shown in Table 1. The catalyst productivity
is defined as the grams of PO formed (including PO which is
subsequently reacted to form PO derivatives) per gram of catalyst
per hour. POE (mole)=moles of PO+moles of PO units in the PO
derivatives. PO/POE=(moles of PO)/(moles of POE).times.100.
Propylene to POE selectivity=(moles of POE)/(moles of propane
formed+moles of POE).times.100.
EXAMPLES 9-14
Propylene Epoxidation with Catalysts B, C, D, E, F, G
[0036] The procedure of Example 8 is repeated except that Catalysts
B, C, D, E, F, G are used respectively instead of Catalyst A.
Results are shown in Table 1.
TABLE-US-00001 TABLE 1 Epoxidation of Propylene Example 8 9 10 11
12 13 14 Pd--Au Catalyst A B C D E F G Support FN-1 FN-1 FN-1 FP-3
FP-3 FW-14 Anatase Support Surface Area (m.sup.2/g) 24 24 24 2 2
0.4 28 Calcination Temperature (.degree. C.) 300 550 650 300 550
300 550 Catalyst Productivity, 0.57 0.49 0.46 0.46 0.43 0.43 0.47 g
POE/g cat/h PO/POE, 88 90 91 90 90 91 90 % (mole/mole) Propylene to
POE Selectivity, 56 77 84 63 75 65 80 % (mole/mole) Hydrogen to POE
Selectivity, 18 23 27 25 29 21 34 % (mole/mole) Oxygen to POE
Selectivity, 37 45 43 38 42 31 38 % (mole/mole)
* * * * *
References