U.S. patent application number 10/431189 was filed with the patent office on 2004-11-11 for silver-containing catalysts, the manufacture of such silver-containing catalysts, and the use thereof.
Invention is credited to Matusz, Marek, Richard, Michael Alan.
Application Number | 20040224841 10/431189 |
Document ID | / |
Family ID | 33416406 |
Filed Date | 2004-11-11 |
United States Patent
Application |
20040224841 |
Kind Code |
A1 |
Matusz, Marek ; et
al. |
November 11, 2004 |
Silver-containing catalysts, the manufacture of such
silver-containing catalysts, and the use thereof
Abstract
A high activity and high selectivity silver catalyst comprising
silver and, optionally, one or more promoters supported on a
suitable support material having the form of a shaped agglomerate.
The structure of the shaped agglomerate is that of a hollow
cylinder having a small inside diameter compared to the outside
diameter. The catalyst is made by providing the shaped material of
a particular geometry and incorporating the catalytic components
therein. The catalyst is useful in the epoxidation of ethylene.
Inventors: |
Matusz, Marek; (Houston,
TX) ; Richard, Michael Alan; (Fulshear, TX) |
Correspondence
Address: |
Charles W. Stewart
Shell Oil Company
Legal - Intellectual Property
P. O. Box 2463
Houston
TX
77252-2463
US
|
Family ID: |
33416406 |
Appl. No.: |
10/431189 |
Filed: |
May 7, 2003 |
Current U.S.
Class: |
502/347 |
Current CPC
Class: |
B01J 35/026 20130101;
C07D 301/08 20130101; B01J 23/63 20130101; B01J 35/10 20130101;
B01J 23/50 20130101; C07D 301/10 20130101; B01J 37/0213 20130101;
B01J 37/0203 20130101; B01J 35/1009 20130101; B01J 23/683 20130101;
B01J 23/58 20130101; B01J 23/688 20130101 |
Class at
Publication: |
502/347 |
International
Class: |
B01J 023/50 |
Claims
That which is claimed is:
1. A catalyst, comprising: Silver at a high concentration level and
at least one promoter compound, wherein said silver and said at
least one promoter compound are supported on a support material
having a high water absorption.
2. A catalyst as recited in claim 1, wherein said support material
is in the form of a shaped agglomerate having a hollow cylinder
geometric configuration such that the L/D ratio of said shaped
agglomerate is in the range of from about 0.3 to about 1.6 and the
internal diameter is in the range upwardly to about 30 percent of
the outer diameter of said shaped agglomerate.
3. A catalyst as recited in claim 2, wherein said high
concentration level of silver is in the range exceeding 15 weight
percent of the total weight of the said catalyst.
4. A catalyst as recited in claim 3, wherein said high water
absorption is in the range of exceeding 42.5%.
5. A catalyst as recited in claim 4, wherein said support material
further has a surface area in the range of from 0.03 m.sup.2/g to
10 m.sup.2/g.
6. A catalyst as recited in claim 1, wherein said high
concentration level of silver is in the range exceeding 15 weight
percent of the total weight of the said catalyst.
7. A catalyst as recited in claims 1 or 2, wherein said high water
absorption is in the range exceeding 42.5%.
8. A catalyst as recited in claims 1, 2 or 3, wherein said support
material further has a surface area in the range of from 0.03
m.sup.2/g to 10 m.sup.2/g.
9. A catalyst as recited in claim 1, wherein said support material
is in the form of a shaped agglomerate having a hollow cylinder
geometric configuration such that the L/D ratio of said shaped
agglomerate is in the range of from about 0.3 to about 1.6 and the
ratio of internal diameter to outside diameter is in the range of
from 0.01 to 0.25.
10. A catalyst as recited in claim 9, wherein said high
concentration level of silver is in the range exceeding 16 weight
percent of the total weight of the said catalyst.
11. A catalyst as recited in claim 10, wherein said high water
absorption is in the range of exceeding 45%.
12. A catalyst as recited in claim 11, wherein said support
material further has a surface area in the range of from 0.05
m.sup.2/g to 5 m.sup.2/g.
13. A catalyst as recited in claim 1, wherein said high
concentration level of silver is in the range exceeding 16 weight
percent of the total weight of the said catalyst.
14. A catalyst as recited in claims 1 or 9, wherein said high water
absorption is in the range of exceeding 45%.
15. A catalyst as recited in claims 1, 9 or 10, wherein said
support material further has a surface area in the range of from
0.05 m.sup.2/g to 5 m.sup.2/g.
16. A catalyst as recited in claim 1, wherein said support material
is in the form of a shaped agglomerate having a hollow cylinder
geometric configuration such that the L/D ratio of said shaped
agglomerate is in the range of from about 0.3 to about 1.6 and the
ratio of inside diameter to outside diameter is in the range of
from 0.02 to 0.25.
17. A catalyst as recited in claim 16, wherein said high
concentration level of silver is in the range exceeding 17 weight
percent of the total weight of the said catalyst.
18. A catalyst as recited in claim 17, wherein said high water
absorption is in the range of exceeding 46%.
19. A catalyst as recited in claim 18, wherein said support
material further has a surface area in the range of from 0.1
m.sup.2/g to 3 m.sup.2/g.
20. A catalyst as recited in claim 1, wherein said high
concentration level of silver is in the range exceeding 17 weight
percent of the total weight of the said catalyst.
21. A catalyst as recited in claims 1 or 16, wherein said high
water absorption is in the range of exceeding 46%.
22. A catalyst as recited in claims 1, 16 or 17, wherein said
support material further has a surface area in the range of from
0.03 m.sup.2/g to 10 m.sup.2/g.
23. A catalyst, comprising: a shaped support material having a
hollow cylinder geometric configuration such that the L/D ratio of
said shaped support material is in the range of from about 0.3 to
about 1.6 and the internal diameter is in the range upwardly to
about 30 percent of the outer diameter of said shaped support
material; and a silver component, wherein the concentration of
silver in said catalyst is in the range exceeding 15 weight percent
of the total weight of said catalyst.
24. A catalyst as recited in claim 23, wherein said shaped support
material has a water absorption greater than 42.5%.
25. A catalyst as recited in claim 24, wherein said shaped support
material comprises an inorganic oxide having a surface area in the
range of from 0.03 m.sup.2/g to 10 m.sup.2/g.
26. A catalyst as recited in claim 25, wherein the ratio of
internal diameter to outside diameter of said shaped support
material is in the range of from 0.01 to 0.25.
27. A catalyst as recited in claim 26, wherein the concentration of
silver in said catalyst exceeds 16 weight percent.
28. A catalyst as recited in claim 27, wherein said catalyst
further comprises a promoter component.
29. A catalyst as recited in claim 23, wherein said shaped support
material comprises an inorganic oxide having a surface area in the
range of from 0.03 m.sup.2/g to 10 m.sup.2/g.
30. A catalyst as recited in claims 23 or 24, wherein the ratio of
internal diameter to outside of said shaped support material is in
the range of from 0.01 to 0.25.
31. A catalyst as recited in claims 23, 24 or 25, wherein the
concentration of silver in said catalyst exceeds 16 weight percent
of the total weight of said catalyst.
32. A catalyst as recited in claims 23, 24, 25, or 26 wherein said
catalyst further comprises a promoter component.
33. A method, comprising: providing a shaped support material; and
impregnating said shaped support material with a silver-containing
solution such that an amount of silver metal incorporated into said
shaped support material exceeds 15 weight percent of the total
weight of said shaped support material to thereby provide a silver
impregnated shaped support material.
34. A method as recited in claim 33, wherein said impregnating step
is a single impregnation step by which said amount of silver metal
is incorporated into said shaped support material.
35. A method as recited in claim 34, wherein said shaped support
material has a geometric configuration such that the L/D ratio is
in the range of from about 0.3 to about 1.6 and the internal
diameter is in the range upwardly to about 30 percent of the outer
diameter of said shaped catalyst support.
36. A method as recited in claim 35, wherein said shaped material
has a water absorption in the range exceeding 42.5% and wherein
said shaped material comprises an inorganic oxide having a surface
area in the range of from 0.03 m.sup.2/g to 10 m.sup.2/g.
37. A method as recited in claim 33, wherein said shaped support
material has a geometric configuration such that the L/D ratio is
in the range of from about 0.3 to about 1.6 and the internal
diameter is in the range upwardly to about 30 percent of the outer
diameter of said shaped catalyst support.
38. A method as recited in claims 33 or 34, wherein said shaped
material has a water absorption in the range exceeding 42.5% and
wherein said shaped material comprises an inorganic oxide having a
surface area in the range of from 0.03 m.sup.2/g to 10
m.sup.2/g.
39. A method as recited in claim 33, wherein said impregnating step
is a single impregnation step by which said amount of silver metal
that is incorporated into said shaped support material exceeds 16
weight percent.
40. A method as recited in claim 39, wherein said shaped support
material has a geometric configuration such that the L/D ratio is
in the range of from about 0.3 to about 1.6 and the ratio of
internal diameter to outside diameter is in the range of from 0.01
to 0.25.
41. A method as recited in claim 40, wherein said shaped material
has a water absorption in the range exceeding 42.5% and wherein
said shaped material comprises an inorganic oxide having a surface
area in the range of from 0.03 m.sup.2/g to 10 m.sup.2/g.
42. A process for manufacturing ethylene oxide, said process
comprises: Contacting, under suitable epoxidation process
conditions, a feed stream, comprising ethylene and oxygen, with the
catalyst of claim 1.
43. A catalyst composition made by the method of claim 33.
Description
[0001] This invention relates to silver-containing catalyst
compositions that are particularly suitable for use in the
manufacture of such silver-containing catalysts.
[0002] Ethylene oxide is an important industrial chemical used as a
feedstock for making such chemicals as ethylene glycol and
detergents. One method of manufacturing ethylene oxide is by the
catalyzed partial oxidation of ethylene with oxygen. There are
continuing efforts to develop catalysts that can improve the
operating efficiency of such ethylene oxide manufacturing
processes. Some of the desirable properties of an ethylene oxide
catalyst include good selectivity and good activity.
[0003] It is, thus, an object of this invention to provide a
catalyst that has certain desirable catalytic properties that make
it particularly suitable for use in the manufacture of ethylene
oxide.
[0004] It is another object of this invention to provide a method
of making a catalyst that exhibits at least some of the
aforementioned desirable catalytic properties.
[0005] Yet another object of this invention is to provide an
economically efficient process for manufacturing ethylene oxide by
utilizing a catalyst having certain desirable catalytic
properties.
[0006] Other aspects, objects and the several advantages of the
invention will become more apparent in light of the following
disclosure.
[0007] According to one invention, a catalyst is provided which has
a high silver concentration and at least one promoter compound. The
silver and promoter compound are supported on a support material
having a high water pore volume.
[0008] According to another invention, a method is provided for
making a catalyst by providing a shaped support material and
impregnating the shaped support material with a silver-containing
solution such that the amount of silver metal in the shaped support
material exceeds 15 weight percent of the total weight of the
shaped support material. The silver impregnated shaped support
material is then heat treated to provide the catalyst.
[0009] According to yet another invention, the above described
catalyst or catalyst made by the above-described method is used in
a process for manufacturing ethylene oxide by contacting the
catalyst, under suitable epoxidation process conditions, with a
feed stream that comprises ethylene and oxygen.
[0010] The catalyst composition of the present invention is a novel
combination of catalytic components and support material. The
support material has specific physical properties and is preferably
formed into a shaped agglomerate of the support material having a
hollow cylinder geometric configuration or structure with a small
internal diameter relative to the outer diameter of the
cylinder.
[0011] The support material of the catalyst composition can be any
porous refractory material that is relatively inert in the presence
of ethylene oxidation feeds, products and reaction conditions;
provided, such support material has the physical properties
required for the inventive catalyst composition especially when
used to support the catalytic components of the inventive
composition. Generally, the support material is an inorganic oxide
which can include, for example, alumina, silicon carbide, silica,
zirconia, magnesia, silica-alumina, silica-magnesia,
silica-titania, alumina-titania, alumina-magnesia,
alumina-zirconia, thoria, silica-titania-zirconia and various
clays.
[0012] The preferred support material comprises alumina preferably
of a high purity of at least 90 weight percent alumina and, more
preferably, at least 98 weight percent alumina. Among the various
available forms of alumina alpha-alumina is the most preferred.
[0013] An important aspect of the inventive catalyst composition is
for the support material to have a high water absorption value
generally exceeding about 40%. This high water absorption value
allows for the loading of a greater amount of silver onto the
support material than can be loaded onto other inorganic oxide
materials that have a lower value for water absorption. It has,
thus, been found that for the inventive catalyst composition it is
important for the water absorption of the support material to be
greater than 42.5%, preferably, greater than 45% and, most
preferably, greater than 46%.
[0014] As used herein, the term "water absorption" means the value
as determined by test procedure ASTM C393, which is incorporated
herein by reference. Water absorption can be expressed as the
weight of the water that can be absorbed into the pores of the
carrier, relative to the weight of the carrier.
[0015] The surface area of the support material as measured by the
B.E.T. method can be in the range of from 0.03 m.sup.2/g to 10
m.sup.2/g, preferably from 0.05 m.sup.2/g to 5 m.sup.2 /g and most
preferably from 0.1 m.sup.2/g to 3 m.sup.2/g. The B.E.T. method of
measuring surface area has been described in detail by Brunauer,
Emmet and Teller in J. Am. Chem. Soc. 60 (1938) 309-316, which is
incorporated herein by reference.
[0016] Another important aspect of the inventive catalyst
composition is for the support material to be in the form of a
shaped agglomerate, and it is particularly important for the shaped
agglomerate of support material to have a hollow cylinder geometric
configuration with an inner diameter, or bore size, that is small
relative to the outer diameter of the hollow cylinder. The smaller
bore diameter helps provide for an improvement in the average crush
strength of the agglomerate by offsetting the loss in crush
strength that results from using a support material having a
greater porosity (i.e. water absorption). Another benefit from the
smaller bore diameter is that it provides for packing a greater
amount of support material into the same volume, i.e., packing
density, thus, allowing for more silver to be loaded into the same
volume.
[0017] While it is an important aspect of the invention for the
bore size of the shaped agglomerate to be small relative to the
outer diameter of the shaped agglomerate, it is also important for
the inside bore of the shaped agglomerate to have at least some
dimension. It has been found that the void space defined by the
inside bore diameter provides for certain benefits in the
manufacturing of the inventive catalyst and its catalytic
properties. While not wanting to be bound to any particular theory,
it is believed, however, that the void space provided by the inside
bore diameter of the hollow cylinder allows for improved carrier
impregnation and catalyst drying. The catalytic benefits associated
with the inventive catalyst is demonstrated and discussed in more
detail elsewhere herein.
[0018] The hollow cylinder geometric configuration can be defined
by an outer diameter, an inner diameter, or bore diameter, and a
length. It is understood that these dimensions are nominal and
approximate, since, methods of manufacturing the shaped
agglomerates are not necessarily precise. The hollow cylinder
should have a length-to-outside diameter ratio in the range of from
about 0.3 to about 2.0, preferably from about 0.5 to about 1.6 and,
most preferably, from 0.9 to 1.1. An important, if not critical
feature of the invention is for the bore diameter to be small
relative to the outside diameter of the hollow cylinder. For
instance, the ratio of bore diameter-to-outside diameter can range
upwardly to 0.3, preferably, from 0.01 to 0.25 and, most
preferably, from 0.02 to 0.2.
[0019] In addition to the support material that is formed into an
agglomerate having a specific geometric configuration, incorporated
into the support material is at least a catalytically effective
amount of silver and, optionally, one or more promoters and,
optionally, one or more copromoters. Thus, the inventive catalyst
comprises a shaped support material, a catalytically effective
amount of silver and, optionally, one or more promoters and,
optionally, one or more copromoters.
[0020] Another particularly important feature of the inventive
catalyst is for the support to be highly loaded with silver.
Indeed, it is the combination of using a high porosity support
material having a shaped configuration that, in combination, helps
provide for the high silver loading. The silver loading is
generally such that the amount of silver in the catalyst
composition exceeds about 15 weight percent based on the total
weight of the catalyst or even exceeding 16 weight percent.
Preferably, however, the silver content of the catalysts should
exceed 17 weight percent and, most preferably, 18 weight
percent.
[0021] In general, the catalyst of the present invention is
prepared by impregnating the shaped agglomerate of support material
with silver and, optionally, one or more promoters, such as, for
example, rare earths, magnesium, rhenium and alkali metals
(lithium, sodium, potassium, rubidium and cesium) and, optionally,
one or more copromoters, such as, for example, sulfur, molybdenum,
tungsten and chromium. Among the promoter components that can be
incorporated into the shaped agglomerate of support material,
rhenium and the alkali metals, in particular, the higher alkali
metals, such as potassium, rubidium and cesium, are preferred. Most
preferred among the higher alkali metals is cesium. Either the
rhenium promoter may be used without an alkali metal promoter being
present or an alkali metal promoter may be used without a rhenium
promoter being present or a rhenium promoter and an alkali metal
promoter can both be present in the catalyst system. The
copromoters can include sulfur, molybdenum, tungsten, and
chromium.
[0022] Silver is incorporated into the shaped agglomerate of
support material by contacting it with a silver solution formed by
dissolving a silver salt, or silver compound, or silver complex in
a suitable solvent. The contacting or impregnation is preferably
done in a single impregnation step whereby the silver is deposited
onto the shaped agglomerate so as to provide, for instance, at
least about 15 weight percent silver, based on the total weight of
the catalyst.
[0023] The one or more promoters can also be deposited on the
shaped agglomerate either prior to, coincidentally with, or
subsequent to the deposition of the silver, but, preferably, the
one or more promoters are deposited on the shaped agglomerate
coincidentally or simultaneously with the silver.
[0024] Promoting amounts of alkali metal or mixtures of alkali
metal can be deposited on a shaped agglomerate support using a
suitable solution. Although alkali metals exist in a pure metallic
state, they are not suitable for use in that form. They are used as
ions or compounds of alkali metals dissolved in a suitable solvent
for impregnation purposes. The shaped agglomerate is impregnated
with a solution of alkali metal promoter ions, salt(s) and/or
compound(s) before, during or after impregnation of the silver ions
or salt(s), complex(es), and/or compound(s) has taken place. An
alkali metal promoter may even be deposited on the shaped
agglomerate after the silver component has been reduced to metallic
silver.
[0025] The promoting amount of alkali metal utilized will depend on
several variables, such as, for example, the surface area and pore
structure and surface chemical properties of the carrier used, the
silver content of the catalyst and the particular ions and their
amounts used in conjunction with the alkali metal cation.
[0026] The amount of alkali metal promoter deposited upon the
shaped agglomerate or present on the catalyst is generally in the
range of from about 10 parts per million to about 3000 parts per
million, preferably between about 15 parts per million and about
2000 parts per million and more preferably, between about 20 parts
per million and about 1500 parts per million by weight of total
catalyst.
[0027] The alkali metal promoters are present on the catalysts in
the form of cations (ions) or compounds or complexes or surface
compounds or surface complexes rather than as the extremely active
free alkali metals, although for convenience purposes in this
specification and claims they are referred to as "alkali metal" or
"alkali metal promoters" even though they are not present on the
catalyst as metallic elements. For purposes of convenience, the
amount of alkali metal deposited on the support or present on the
catalyst is expressed as the metal. Without intending to limit the
scope of the invention, it is believed that the alkali metal
compounds are oxidic compounds. More particularly, it is believed
that the alkali metal compounds are probably in the form of mixed
surface oxides or double surface oxides or complex surface oxides
with the aluminum of the support and/or the silver of the catalyst,
possibly in combination with species contained in or formed from
the reaction mixture, such as, for example, chlorides or carbonates
or residual species from the impregnating solution(s).
[0028] The shaped agglomerate can also be impregnated with rhenium
ions, salt(s), compound(s), and/or complex(es). This may be done at
the same time that the alkali metal promoter is added, or before or
later; or at the same time that the silver is added, or before or
later. Preferably, rhenium, alkali metal, and silver are in the
same impregnating solution, although it is believed that their
presence in different solutions will still provide suitable
catalysts.
[0029] The preferred amount of rhenium, calculated as the metal,
deposited on or present on the shaped agglomerate or catalyst
ranges from about 0.1 micromoles (.mu.mole) per gram to about 10
micromoles per gram, more preferably from about 0.2 micromoles per
gram to about 5 micromoles per gram of total catalyst, or,
alternatively stated, from about 19 parts per million to about 1860
parts per million, preferably from about 37 parts per million to
about 930 parts per million by weight of total catalyst. The
references to the amount of rhenium present on the catalyst are
expressed as the metal, irrespective of the form in which the
rhenium is actually present.
[0030] The rhenium compound used in the preparation of the instant
catalyst includes rhenium compounds that can be solubilized in an
appropriate solvent. Preferably, the solvent is a water-containing
solvent. More preferably, the solvent is the same solvent used to
deposit the silver and the alkali metal promoter.
[0031] Examples of suitable rhenium compounds used in making the
inventive catalyst include the rhenium salts such as rhenium
halides, the rhenium oxyhalides, the rhenates, the perrhenates, the
oxides and the acids of rhenium. A preferred compound for use in
the impregnation solution is the perrhenate, preferably ammononium
perrhenate. However, the alkali metal perrhenates, alkaline earth
metal perrhenates, silver perrhenates, other perrhenates and
rhenium heptoxide can also be suitably utilized. Rhenium heptoxide,
Re.sub.2O.sub.7, when dissolved in water, hydrolyzes to perrhenic
acid, HReO.sub.4, or hydrogen perrhenate. Thus, for purposes of
this specification, rhenium heptoxide can be considered to be a
perrhenate, i.e., ReO.sub.4.
[0032] It is also understood that there are many rhenium compounds
that are not soluble in water but can be solubilized in water by
utilizing various acids, bases, peroxides, alcohols, and the like.
After solubilization, these compounds can be used, for example,
with an appropriate amount of water or other suitable solvent to
impregnate the shaped agglomerate. Of course, it is also understood
that upon solubilization of many of these compounds, the original
compound no longer exists in the same form after solubilization.
For example, rhenium metal is not soluble in water. However, it is
soluble in concentrated nitric acid as well as in hydrogen peroxide
solution. Thus, by using an appropriate reactive solvent, one could
use rhenium metal to prepare a solubilized rhenium-containing
impregnating solution. In a preferred embodiment of the instant
invention, the rhenium present on the catalyst is present in a form
that is extractable in a dilute aqueous base solution.
[0033] The one or more copromoters can be deposited on the shaped
agglomerate by any suitable manner known to those skilled in the
art. The copromoter is deposited on the shaped agglomerate either
prior to, coincidentally with, or subsequent to the deposition of
the silver, but preferably, the one or more copromoters are
deposited on the shaped agglomerate coincidentally or
simultaneously with the silver. A copromoting amount of copromoter
is deposited on the shaped agglomerate and can generally be in the
range of from about 0.01 to about 25, or more, .mu.moles per gram
of total catalyst.
[0034] The catalysts according to the present invention have a
particularly high activity and high selectivity for ethylene oxide
production in the direct oxidation of ethylene with molecular
oxygen to ethylene oxide. For instance, the inventive catalyst can
have an initial selectivity of at least about 86.5 mole percent,
preferably, at least 87 mole percent and, most preferably, at least
88.5 mole percent.
[0035] As it is used herein with reference to the selectivity of a
catalyst, the term "selectivity", S.sub.w, means the mole percent
(%) of the desired ethylene oxide formed relative to the total of
ethylene converted at a given work rate, w, for a catalyst with the
work rate being defined as the amount of ethylene oxide produced
per unit volume of catalyst (e.g., kg per m.sup.3) per hour. As it
is used herein with reference to the activity of a catalyst, the
term "activity", T.sub.w, means the temperature needed to reach a
given work rate.
[0036] The term "initial selectivity" referred to herein means the
selectivity of the given catalyst when it has been used for less
than two weeks in accordance with the following described standard
testing procedure. The initial selectivity of a given catalyst is
determined by measuring the selectivity of the catalyst using a
standard testing procedure. In this standard testing procedure, a
crushed catalyst (14-20 mesh) is placed within the 1/4 inch
diameter stainless steel U-tube of a micro-reactor operated under
certain specified process conditions. A standard feed of 30 mole
percent ethylene, 5 mole percent carbon dioxide, and 8 mole percent
oxygen, and 57 mole percent nitrogen is introduced into the
micro-reactor at a pressure of 210 psig and at such a rate as to
provide a gaseous hourly space velocity of 3300 hr.sup.-1. The
selectivity, Sw, and activity, Tw, are determined for a work rate
of 200 kg ethylene oxide yield per hour per cubic meter of
catalyst. The selectivity is presented in terms of mole percent,
and the activity is presented in terms of temperature in degrees
centigrade.
[0037] The conditions for carrying out the epoxidation oxidation
reaction in the presence of the inventive catalysts according to
the present invention broadly comprise those already described in
the prior art. This applies, for example, to suitable temperatures,
pressures, residence times, diluent materials such as nitrogen,
carbon dioxide, steam, argon, methane or other saturated
hydrocarbons, to the presence of moderating agents to control the
catalytic action, for example, 1-2, dichloroethane, vinyl chloride,
ethyl chloride or chlorinated polyphenyl compounds, to the
desirability of employing recycle operations or applying successive
conversions in different reactors to increase the yields of
ethylene oxide, and to any other special conditions which may be
selected in processes for preparing ethylene oxide. Pressures in
the range of from atmospheric to about 500 psig are generally
employed. Higher pressures, however, are not excluded. The
molecular oxygen employed as reactant can be obtained from any
suitable source including conventional sources. A suitable oxygen
charge can include relatively pure oxygen, or a concentrated oxygen
stream comprising oxygen in major amount with lesser amounts of one
or more diluents, such as nitrogen and argon, or any other
oxygen-containing stream, such as air. The use of the present
catalysts in ethylene oxide reactions is in no way limited to the
use of specific conditions among those that are known to be
effective.
[0038] For purposes of illustration only, the following table shows
the range of conditions that are often used in current commercial
ethylene oxide reactor units.
1 TABLE I *GHSV 1500-10,000 Inlet Pressure 150-400 psig Inlet Feed
Ethylene 1-40% Oxygen 3-12% Carbon dioxide 0-15% Ethane 0-3% Argon
and/or methane and/or nitrogen balance Diluent chlorohydrocarbon
moderator 0.3-20 ppmv total Coolant temperature 180-315.degree. C.
Catalyst temperature 180-325.degree. C. O.sub.2 conversion level
10-60% Ethylene Oxide (EO) Production 2-20 lbs. EO/cu. ft. (Work
Rate) catalyst/hr. *Cubic feet of gas at standard temperature and
pressure passing over one cubic foot of packed catalyst per
hour.
[0039] In a preferred application, ethylene oxide is produced when
an oxygen-containing gas is contacted with ethylene in the presence
of the inventive catalysts under suitable epoxidation reaction
conditions such as at a temperature in the range of from about
180.degree. C. to about 330.degree. C., and, preferably,
200.degree. C. to 325.degree. C., and a pressure in the range of
from atmospheric to about 500 psig and, preferably, from 150 psig
to 400 psig.
[0040] The following examples are intended to illustrate the
advantages of the present invention and are not intended to unduly
limit the scope of the invention.
EXAMPLE I
[0041] This Example I describes the preparation of a stock silver
impregnation solution used for impregnating various support
materials as described in the following examples.
[0042] In a 5-liter stainless steel beaker 415 grams of reagent
grade sodium hydroxide was dissolved in 2340 ml of deionized water.
The temperature of the solution was adjusted to about 50.degree. C.
In a 4-liter stainless steel beaker 1699 grams of silver nitrate
was dissolved in 2100 ml of deionized water. The temperature of the
solution was adjusted to about 50.degree. C. The sodium hydroxide
solution was slowly added to the silver nitrate solution with
stirring while the temperature was maintained at about 50.degree.
C. The resulting slurry was stirred for about 15 minutes. The pH of
the solution was maintained at above 10 by the addition of NaOH
solution as required. A washing procedure was used which included
removing liquid by the use of a filter wand followed by the
replacement of the removed liquid with an equivalent volume of
deionized water. This washing procedure was repeated until the
conductivity of the filtrate dropped below 90 micro-mho/cm. After
the completion of the last wash cycle, 1500 ml of deionized water
was added and followed by the addition of 630 grams of oxalic acid
dihydrate (4.997 moles) in increments of 100 grams while stirring
and maintaining the solution at about 40.degree. C. (.+-.5.degree.
C.). The pH of the solution was monitored during the addition of
the last 130 grams of oxalic acid dihydrate to ensure that it did
not drop below 7.8 for an extended period of time. Water was
removed from the solution with a filter wand and the slurry was
cooled to less than 30.degree. C. Slowly added to the solution was
732 grams of 92% ethylenediamine. The temperature was maintained
below 30.degree. C. during this addition. A spatula was used to
manually stir the mixture until enough liquid was present to
mechanically stir. The final solution was used as a stock silver
impregnation solution for preparing the catalysts of Example
III.
EXAMPLE II
[0043] This Example II presents information concerning the
properties and geometric configuration of the three types of
carrier supports (i.e., Carrier A, Carrier B, and Carrier C) used
in the preparation of the catalysts as described in Example III.
Presented in the following Table II are certain properties of each
of the carrier supports.
2TABLE II Properties of Carrier Supports Carrier A Carrier B
Carrier C Properties Water Absorption (%) 39.2 45.6 46.5 Packing
Density 50.3 45.5 52.7 ASTM Attrition Loss, % 10.8 14.6 14.7
Average Crush Strength 28.6 21.4 29.3 Surface Area 0.80 0.78 0.77
Geometric Configuration Nominal Size (mm) 8 8 8 Average Length 8.1
8.1 7.7 Length, Range 7.6-8.8 6.6-8.6 Diameter 8.5 8.5 8.6 Bore
Size, mm 3.8 3.8 1.02 Length/Outside Diameter approx. 1 0.95 0.90
Internal Diameter, mm 3.8 3.8 1.0
[0044] Each carrier support presented in the above Table II had a
nominal size of 8 mm and a hollow cylinder geometric configuration.
The inner diameter of both Carrier A and Carrier B was 3.8 mm,
while the inner diameter of Carrier C was only 1 mm. The water pore
volumes of Carrier B and Carrier C were significantly greater than
the water pore volume of Carrier A. This explains the reduction in
crush strength and packing density of Carrier B relative to Carrier
A; however, with the reduction of the inner diameter of Carrier C
relative to both Carrier A and Carrier B, the crush strength and
packing density are improved such that these properties have values
that exceed such values for Carrier A.
EXAMPLE III
[0045] This Example III describes the preparation of the comparison
catalyst and the inventive catalysts and certain of their physical
properties.
Catalyst A
[0046] The impregnation solution for preparing Catalyst A was made
by mixing 153 grams of silver stock solution of specific gravity
1.5673 g/cc with a solution of 0.1235 g of NH.sub.4ReO.sub.4 in 2 g
of 1:1 EDA/H.sub.2O, 0.0574 g of ammonium metatungstate dissolved
in 2 g of 1:1 ammonia/water and 0.3174 g LiNO.sub.3 dissolved in
water. Additional water was added to adjust the specific gravity of
the solution to 1.465 g/cc. 50 grams of such doped solution was
mixed with 0.1016 g of 50% CsOH solution. This final impregnating
solution was used to prepare Catalyst A. 30 grams of Carrier A was
evacuated to 20 mm Hg for 1 minute and the final impregnating
solution was added to Carrier A while under vacuum, then the vacuum
was released and the carrier allowed to contact the liquid for 3
minutes. The impregnated Carrier A was then centrifuged at 500 rpm
for 2 minutes to remove excess liquid. Impregnated Carrier A
pellets were placed in a vibrating shaker and dried in flowing air
at 250.degree. C. for 51/2 minutes. The final Catalyst A
composition was 13.2% Ag, 460 ppm Cs/g catalyst, 1.5 .mu.mole Re/g
catalyst, 0.75 .mu.mole W/g catalyst, and 15 .mu.mole Li/g
catalyst.
Catalyst B
[0047] The impregnation solution for preparing Catalyst B was made
by mixing 153 grams of silver stock solution of specific gravity
1.589 g/cc with a solution of 0.1051 g of NH.sub.4ReO.sub.4 in 2 g
of 1:1 EDA/H.sub.20, 0.0488 g of ammonium metatungstate dissolved
in 2 g of 1:1 ammonia/water and 0.270 g LiNO.sub.3 dissolved in
water. Additional water was added to adjust the specific gravity of
the solution to 1.588 g/cc. 50 grams of such doped solution was
mixed with 0.0940 g of 50% CsOH solution. This final impregnating
solution was used to prepare Catalyst B. 30 grams of Carrier B was
evacuated to 20 mm Hg for 1 minute and the final impregnating
solution was added to Carrier B while under vacuum, then the vacuum
was released and the carrier allowed to contact the liquid for 3
minutes. The impregnated Carrier B was then centrifuged at 500 rpm
for 2 minutes to remove excess liquid. Impregnated Carrier B
pellets were placed in a vibrating shaker and dried in flowing air
at 250.degree. C. for 51/2 minutes. The final Catalyst B
composition was 17.5% Ag, 500 ppm Cs/g catalyst, 1.5 .mu.mole Re/g
catalyst, 0.75 .mu.mole W/g catalyst, and 15 .mu.mole Li/g
catalyst.
Catalyst C
[0048] The impregnation solution for preparing Catalyst C was made
by mixing 204 grams of silver stock solution of specific gravity
1.573 g/cc with a solution of 0.1378 g of NH.sub.4ReO.sub.4 in 2 g
of 1:1 EDA/H.sub.2O, 0.0064 g of ammonium metatungstate dissolved
in 2 g of 1:1 ammonia/water and 0.3542 g LiNO.sub.3 dissolved in
water. Additional water was added to adjust the specific gravity of
the solution to 1.558 g/cc. 50 grams of such doped solution was
mixed with 0.0850 g of 50% CsOH solution. This final impregnating
solution was used to prepare Catalyst C. 30 grams of Carrier C was
evacuated to 20 mm Hg for 1 minute and the final impregnating
solution was added to Carrier C while under vacuum, then the vacuum
was released and the carrier allowed to contact the liquid for 3
minutes. The impregnated Carrier C was then centrifuged at 500 rpm
for 2 minutes to remove excess liquid. Impregnated Carrier C
pellets were placed in a vibrating shaker and dried in flowing air
at 250.degree. C. for 7 minutes. The final Catalyst C composition
was 17.8% Ag, 460 ppm Cs/g catalyst, 1.5 .mu.mole Re/g catalyst,
0.75 .mu.mole W/g catalyst, and 15 .mu.mole Li/g catalyst.
[0049] Presented in Table III are the silver loadings of each of
the catalysts. It is significant to note that the silver component
of the inventive catalyst systems was incorporated into the support
material by use of a single impregnation instead of by use of
multiple impregnations. Catalyst B includes a significantly higher
amount of silver than does Catalyst A. This is thought to be due to
the higher water absorption of Carrier B as compared to Carrier A.
As for Catalyst C, while it contains close to the same weight
percent silver as does Catalyst B, a greater total amount of silver
is able to be loaded into a given reactor volume with Catalyst C as
opposed to Catalyst A or Catalyst B due to the modified
geometry.
3TABLE III Silver Content of Catalyst Systems Weight % Silver in
Catalyst Catalyst A 13.2 Catalyst B 17.5 Catalyst C 17.8
EXAMPLE IV
[0050] This Example IV describes the procedure for testing certain
of the catalytic properties, such as, selectivity and activity, of
the catalysts described in Example III.
[0051] Catalysts A, B and C were tested for their ability to
produce ethylene oxide from a feed containing ethylene and oxygen.
To do this, 4 to 5 g of crushed catalyst was loaded into a 1/4 inch
stainless steel U-shaped tube. The tube was immersed in a molten
metal bath (heat medium) and the ends were connected to a gas flow
system. The weight of catalyst used and the inlet gas flow rate
were adjusted to give a gas hourly space velocity of 3300 Nl/(1.h),
as calculated for uncrushed catalyst. As the catalyst packing
density and silver loading changes, the amount of catalyst loaded
in the test reactor was changed to reflect larger amounts of silver
packed into a reactor. The catalyst loadings were as follows:
Catalyst A (comparative) 4.2 grams, Catalyst B (invention) 4.01 g
and Catalyst C (invention) 4.66 g. The gas flow was 16.9 Nl/h. The
inlet gas pressure was 1550 kPa. The catalysts were treated with
nitrogen at 225.degree. C. for 2 hours prior to testing. The
testing gas mixture passed through the catalyst bed, in a
"once-through" operation, consisted of 30% v ethylene, 8% v oxygen,
5% v carbon dioxide, 57% v nitrogen and 2.0 to 6.0 parts by million
by volume (ppmv) ethyl chloride. Ethyl chloride concentration was
adjusted to obtain maximum selectivity.
4TABLE IV Catalytic Performance of Catalysts Selectivity Activity
Percent (%) Temp (.degree. C.) Catalyst A 88.0 262 Catalyst B 89.1
263 Catalyst C 89.4 254
[0052] As can be seen from the catalyst performance data presented
in Table IV, Catalyst B demonstrates an improved selectivity
compared to that of Catalyst A having a selectivity of 89.1% at
263.degree. C. versus a selectivity of 88.0% at 262.degree. C. for
Catalyst A. As the term is used herein, "selectivity" means the
mole percent of the ethylene oxide formed relative to the total
ethylene converted. It is believed that this improvement in
selectivity is attributable to the high water absorption of
Catalyst B relative to Catalyst A that permits the packing of more
silver into the reactor to thereby provide for greater
selectivity.
[0053] Catalyst C demonstrates an even greater improvement in
selectivity relative to Catalyst A than does Catalyst B, with
Catalyst C having a selectivity of 89.4% at 254.degree. C. versus
88.0% at 262. Catalyst C also demonstrates a greater activity than
both Catalyst A and Catalyst B by requiring a significantly lower
reaction temperature that gives a significantly greater
selectivity. It is believed that the improved selectivity of
Catalyst C over that of both Catalyst A and Catalyst B is
attributable to the greater amount of silver that can be packed
into a reactor due to the high silver loading achievable with the
catalyst having a higher water absorption. The improved activity is
believed to result from the use of a carrier support material
having a hollow cylinder geometric configuration with a small bore
diameter in the manufacture of the catalyst.
[0054] While this invention has been described in terms of the
presently preferred embodiment, reasonable variations and
modifications are possible by those skilled in the art. Such
variations and modifications are within the scope of the described
invention and the appended claims.
* * * * *