U.S. patent application number 14/735447 was filed with the patent office on 2015-10-01 for methane aromatization catalyst, method of making and method of using the catalyst.
The applicant listed for this patent is Shell Oil Company. Invention is credited to Armin LANGE DE OLIVEIRA, Peter Tanev TANEV.
Application Number | 20150274610 14/735447 |
Document ID | / |
Family ID | 44914954 |
Filed Date | 2015-10-01 |
United States Patent
Application |
20150274610 |
Kind Code |
A1 |
TANEV; Peter Tanev ; et
al. |
October 1, 2015 |
METHANE AROMATIZATION CATALYST, METHOD OF MAKING AND METHOD OF
USING THE CATALYST
Abstract
A catalyst for converting methane to aromatic hydrocarbons is
described herein. The catalyst comprises an active metal or a
compound thereof, and an inorganic oxide support wherein the active
metal is added to the support in the form of metal oxalate. The
metal oxalate-derived catalyst exhibits superior performance in the
conversion of methane-rich feed to aromatics products relative to
catalysts prepared from non-oxalate metal precursors. A method of
making the catalyst and a method of using the catalyst are also
described.
Inventors: |
TANEV; Peter Tanev; (Katy,
TX) ; LANGE DE OLIVEIRA; Armin; (Heidelberg,
DE) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
Shell Oil Company |
Houston |
TX |
US |
|
|
Family ID: |
44914954 |
Appl. No.: |
14/735447 |
Filed: |
June 10, 2015 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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13105499 |
May 11, 2011 |
9079169 |
|
|
14735447 |
|
|
|
|
61333995 |
May 12, 2010 |
|
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Current U.S.
Class: |
585/417 ;
502/62 |
Current CPC
Class: |
B01J 23/28 20130101;
C07C 2/76 20130101; C07C 2523/34 20130101; C07C 2523/20 20130101;
C07C 2523/75 20130101; B01J 37/08 20130101; C07C 2523/26 20130101;
C07C 2523/30 20130101; B01J 35/023 20130101; C07C 2529/65 20130101;
B01J 37/086 20130101; C07C 2523/72 20130101; C07C 2523/14 20130101;
C07C 2529/40 20130101; B01J 29/076 20130101; B01J 37/0203 20130101;
B01J 29/48 20130101; C07C 2523/28 20130101; C07C 2521/08 20130101;
C07C 2521/04 20130101; B01J 37/0201 20130101; C07C 2523/36
20130101; C07C 2/76 20130101; C07C 2531/26 20130101; C07C 2523/06
20130101; C07C 15/04 20130101; Y02P 20/52 20151101; C07C 2523/50
20130101; C07C 2523/46 20130101; C07C 2523/10 20130101; C07C
2523/08 20130101; C07C 2523/755 20130101; B01J 31/26 20130101; C07C
2521/06 20130101; C07C 2523/22 20130101; C07C 2523/42 20130101;
C07C 2523/745 20130101 |
International
Class: |
C07C 2/76 20060101
C07C002/76; B01J 37/08 20060101 B01J037/08; B01J 37/02 20060101
B01J037/02; B01J 31/26 20060101 B01J031/26 |
Claims
1. A process for preparing a methane aromatization catalyst
comprising: contacting an active metal oxalate with an inorganic
oxide support to form a mixture, and calcining the mixture.
2. A process as claimed in claim 1 wherein the active metal oxalate
is in the form of a solution that is used to impregnate the
inorganic support.
3. A process as claimed in claim 1 wherein the active metal
compound comprises molybdenum.
4. A process as claimed in claim 1 wherein the inorganic oxide
support is a zeolite or zeolite-containing support.
5. A process as claimed in claim 1 wherein the support comprises
ZSM-5 type zeolite
6. A process as claimed in claim 1 wherein the support contains
zeolite and a binder
7. A process as claimed in claim 1 wherein contacting the metal
oxalate with the inorganic oxide support is carried out at a
temperature in the range of from 0.degree. C. to 100.degree. C.
8. A process as claimed in claim 1 wherein contacting the metal
oxalate with the inorganic oxide support is carried out at a
temperature in the range of from 15.degree. C. to 40.degree. C.
9. A process as claimed in claim 1 further comprising a drying step
before the calcining.
10. A process as claimed in claim 9 wherein the drying and
calcining comprises: a. subjecting the impregnated support to a
temperature of from 70.degree. C. to 120.degree. C. for at least 20
minutes; b. increasing the temperature at a rate of from 1.degree.
C. to 10.degree. C. per minute to a temperature of from 275.degree.
C. to 325.degree. C.; c. maintaining the temperature achieved in
step (b) for at least 20 min; d. increasing the temperature at a
rate of from 1.degree. C. to 30.degree. C. per minute to a
temperature of from 475.degree. C. to 650.degree. C.; and e.
maintaining the temperature achieved in step (d) for at least 20
min.
11. A process as claimed in claim 16 wherein the drying and
calcining comprises: a. subjecting the impregnated support to a
temperature of from 70.degree. C. to 120.degree. C. for from 20
minutes to 240 minutes; b. increasing the temperature at a rate of
from 1.degree. C. to 10.degree. C. per minute to a temperature of
from 275.degree. C. to 325.degree. C.; c. maintaining the
temperature achieved in step (b) for from 20 minutes to 240
minutes; d. increasing the temperature at a rate of from 1.degree.
C. to 30.degree. C. per minute to a temperature of from 475.degree.
C. to 550.degree. C.; and e. maintaining the temperature achieved
in step (d) for from 20 minutes to 240 minutes.
12. A process as claimed in claim 8 further comprising cooling the
impregnated support after calcination.
13. A process for producing aromatic hydrocarbons comprising
contacting a gas stream comprising methane with a catalyst
comprising molybdenum where the catalyst was prepared by contacting
a molybdenum oxalate with a zeolite-containing support.
14. A process as claimed in claim 13 wherein the gas stream
comprising methane has a methane concentration of from 75 to 100
volume percent.
15. A process as claimed in claim 13 wherein the gas stream
comprising methane is derived from biogas.
16. A process as claimed in claim 13 wherein the gas stream
containing methane is natural gas.
Description
[0001] This application is a divisional of U.S. Non-Provisional
application Ser. No. 13/105,499, filed May 11, 2011 which claims
the benefit of U.S. Provisional Application Ser. No. 61/333,995,
filed on May 12, 2010, the entire disclosure of which is herein
incorporated by reference.
FIELD
[0002] This invention relates to a catalyst useful in converting
methane to aromatic hydrocarbons, a method of making the catalyst
and a method of using the catalyst to convert methane to aromatic
hydrocarbons.
BACKGROUND
[0003] The aromatic hydrocarbons (specifically benzene, toluene and
xylenes), are the main high-octane bearing components of the
gasoline pool and important petrochemicals used as building blocks
to produce high value chemicals and a variety of consumer products,
for example, styrene, phenol, polymers, plastics, medicines, and
others. Aromatics are primarily produced from oil-derived refinery
feedstocks in such processes as catalytic reforming and cracking of
heavy naphthas. However, the recent severe oil shortages and price
spikes resulted in severe aromatics shortages and price spikes.
Therefore, there is a need to develop new commercial routes to
produce high value aromatics from highly abundant and cheap
hydrocarbon feedstocks, for example, methane or stranded natural
gas (typically containing about 80-90% methane).
[0004] There are enormous proven stranded natural gas reserves
around the world. According to some estimates, the natural gas
reserves are at least equal to those of oil. However, unlike the
oil reserves which are primarily concentrated in a few oil-rich
countries and are properly and extensively exploited, upgraded and
monetized, the natural gas reserves are much more broadly
distributed around the world and significantly underutilized. Many
developing countries that have significant natural gas reserves
lack the proper infrastructure to exploit them and convert them to
higher value products. Quite often, in such situations, natural gas
is flared to the atmosphere and wasted. Because of the above
reasons, there is enormous economic incentive to develop new
technologies that can efficiently convert methane or natural gas to
higher value chemical products, specifically aromatics.
[0005] In 1993, Wang et al., (Catal. Lett. 1993, 21, 35-41),
discovered that methane can be partially converted to benzene at
atmospheric pressure and a temperature of 700.degree. C. over a
catalyst containing 2.0 wt % molybdenum deposited on H-ZSM-5
zeolite support. Significantly, low methane conversion of less than
10% but very high benzene selectivity of 100% were observed in
these experiments. Subsequently, other researchers repeated the
above work and found that Wang et al. did not quite identify all of
the reaction products (naphthalene and others) and that when all of
the products are identified the benzene selectivity falls in the
range of 60-70%. These other researchers also pointed out that, the
catalyst cokes up and deactivates very rapidly--as manifested by
complete loss of activity after about 4-5 hrs on stream. Since
Wang's discovery, many academic and industrial research groups have
contributed to further developing various aspects of the methane to
benzene catalyst and process technology. Many catalyst formulations
have been prepared and tested and various reactor and process
conditions and schemes have been explored.
[0006] Despite these efforts, there is still no commercial methane
aromatization or methane to benzene catalyst and process. The vast
majority of researchers agree that the main obstacles to developing
and commercializing an efficient, direct methane to benzene process
are the low methane conversion (still remaining at around 7-10%)
and rapid coke formation and catalyst deactivation.
[0007] Therefore, there is a need to develop new methane
aromatization catalysts that provide higher methane conversion at
equal or higher selectivity to benzene relative to the prior art.
Also, there is a need to develop catalysts that exhibit lower
coking and deactivation rates, i.e. better sustain their methane
conversion and benzene selectivity performance over the course of
time (exhibit better stability) relative to the catalysts of the
prior art.
SUMMARY OF THE INVENTION
[0008] The invention provides a methane aromatization catalyst
comprising an active metal or a compound thereof, and an inorganic
oxide support wherein the active metal is added to the support as a
metal oxalate. Preferably, the catalyst comprises molybdenum as the
active metal and a zeolite as the inorganic support.
[0009] The invention further provides a process for preparing a
methane aromatization catalyst comprising: contacting an active
metal oxalate with an inorganic oxide support to form a mixture,
and calcining the mixture.
[0010] The invention still further provides a process for producing
aromatic hydrocarbons comprising contacting a gas stream comprising
methane with a catalyst comprising molybdenum where the catalyst
was prepared by contacting a molybdenum oxalate with a
zeolite-containing support.
BRIEF DESCRIPTION OF DRAWINGS
[0011] FIG. 1 shows the methane (CH.sub.4) conversion versus time
on stream data obtained for the catalysts described in the
Examples.
[0012] FIG. 2 shows the benzene selectivity versus methane
(CH.sub.4)conversion data obtained for the catalysts described in
the Examples.
[0013] FIG. 3 shows the methane (CH.sub.4) conversion versus time
on stream data obtained for the catalysts described in the Examples
after they have been spent and regenerated.
[0014] FIG. 4 shows the benzene selectivity versus methane
(CH.sub.4) conversion data obtained for the catalysts described in
the Examples after they have been spent and regenerated.
DETAILED DESCRIPTION
[0015] The methane aromatization catalyst described here comprises
an active metal and an inorganic oxide support. The active metal
may be any metal that exhibits catalytic activity when contacted
with a stream comprising methane under methane aromatization
conditions. The active metal may be selected from the group
consisting of: vanadium, chromium, manganese, iron, cobalt, nickel,
copper, zinc, gallium, germanium, niobium, molybdenum, ruthenium,
rhodium, silver, tantalum, tungsten, rhenium, platinum and lead and
mixtures thereof. The active metal is preferably molybdenum.
[0016] The inorganic oxide support can be any support that, when
combined with the active metal contributes to the overall catalyst
performance exhibited in the methane aromatization reaction. The
support has to be suitable for treating or impregnating with the
active metal or compound thereof. The inorganic support preferably
has a well developed porous structure with sufficiently high
surface area and pore volume and suitable surface acidity. The
inorganic oxide support may be selected from the group consisting
of: zeolites, non-zeolitic molecular sieves, silica, alumina,
zirconia, titania, yttria, ceria, rare earth metal oxides and
mixtures thereof. The inorganic oxide support contains zeolite as
the primary component. The zeolite may be of a ZSM-5, ZSM-22,
ZSM-8, ZSM-11, ZSM-12 or ZSM-35 zeolite structure type. Preferably,
the support of this invention comprises ZSM-5 zeolite. The ZSM-5
zeolite further may have a SiO.sub.2/Al.sub.2O.sub.3 ratio of 10 to
100. Preferably, the SiO.sub.2/Al.sub.2O.sub.3 ratio of the ZSM-5
zeolite of this invention is in the range of 20-50. Even more
preferably, the SiO.sub.2/Al.sub.2O.sub.3 ratio is from 20 to 40
and most preferably about 30. The zeolite support could further
contain about 10-30% wt of inorganic oxide binder that allows for
shaping of the catalyst in the desired form and for achieving the
high mechanical strength and abrasion resistance desired for
commercial operation. The binder may be selected from the group of
silica, alumina, zirconia, titania, yttria, ceria, rare earth
oxides or mixtures thereof.
[0017] The active metal or compound thereof is added to the support
from a metal oxalate precursor. If the metal oxalate is not
commercially available, the active metal or compound thereof is
reacted with oxalic acid to form the desired metal oxalate
precursor. The metal oxalate precursor can be formed by adding the
necessary amount of metal oxide powder to a solution of oxalic
acid. Preferably, the metal oxide powder is Mo(VI)O.sub.3. The
mixture may be stirred and/or heated as necessary to obtain a clear
solution of the metal oxalate.
[0018] The inorganic oxide support can be mixed with the metal
oxalate to afford a solid state mixture that can then be subjected
to calcination in an oven under dry air flow atmosphere to
evaporate and deposit the active metal in the pores of the zeolite.
This technique is known to those skilled in the art as solid state
ion-exchange. In a more preferred embodiment, the inorganic support
is impregnated with metal oxalate by adding a metal oxalate
precursor solution to a vessel containing the necessary amount of
inorganic oxide support. The support is left in contact with the
solution for a sufficient time to allow the metal oxalate to
penetrate the pores of the support and react with the active
centers of the zeolite.
[0019] Other components or promoters can be added to the support in
various precursor forms and impregnation order to improve various
aspects of the finished catalyst physical or mechanical properties
or catalytic performance. For example, a promoter precursor could
be added to the support in a mixing or impregnation step before,
after or simultaneously with the active metal oxalate.
[0020] The support, now impregnated with metal oxalate, is dried
and calcined to form the finished methane aromatization catalyst of
this invention. The drying and calcination steps typically include
flowing dry air or nitrogen in a volume of from 1 to 60 liters per
hour over the catalyst precursor, preferably from 20 to 50 liters
per hour. The impregnated support may be subjected to a series of
specific heating rates and temperature ramps to complete the
cross-linking of the structure and to form the finished active
metal oxide/zeolite comprising methane aromatization catalyst of
the invention.
[0021] The impregnated support is preferably dried and calcined by
heating it at a temperature of from 80.degree. C. to 120.degree. C.
for a period of time of at least 20 minutes, preferably of from 60
minutes to 180 minutes. The temperature is then increased to from
275.degree. C. to 325.degree. C. at a rate of from 1.degree. C. to
10.degree. C. per minute, preferably from 2 to 4.degree. C. per
minute. That temperature is then maintained for a period of time of
at least 20 minutes, preferably from 60 minutes to 180 minutes.
Then, the temperature is again increased, this time to from
475.degree. C. to 525.degree. C. at a rate of 1.degree. C. to
10.degree. C. per minute, preferably from 2 to 4.degree. C. per
minute. This temperature is then maintained for at least 20
minutes, preferably from 20 minutes to 240 minutes, and even more
preferably of from 120 minutes to 240 minutes.
[0022] The catalyst formed by the above steps is then preferably
cooled to a temperature in the range of from 80.degree. C. to
120.degree. C.
[0023] The methane aromatization catalyst is useful in the reaction
of methane or methane-rich gases, for example, natural gas, to form
aromatic hydrocarbons. Natural gas is defined as a mixture of
saturated hydrocarbons having a carbon number of from 1 to 5,
preferably of from 1 to 4.
[0024] The conversion of methane-containing gas to aromatic
hydrocarbons is typically carried out in a reactor comprising a
catalyst which is active in the conversion of methane to aromatics.
The methane containing gas that is fed to the reactor contains more
than 50% vol. methane, preferably more than 75% vol. methane and
even more preferably of from 75% vol. to 100% vol. methane.
[0025] The conversion of methane-containing gas is carried out at a
space velocity of from 100 to 10000 h.sup.-1, a pressure of from
0.5 to 10 bar and a temperature or from 500 to 850.degree. C. More
preferably, the conversion is carried out at space velocity of from
300 to 3000 h.sup.-1, a pressure of from 0.5 to 5 bar and a
temperature of from 600 to 800.degree. C. Even more preferably, the
conversion is carried out at space velocity of from 500 to 1500
h.sup.-1, a pressure of from 0.5 to 1 bar and a temperature of from
650 to 750.degree. C. Various co-feeds such as CO, CO.sub.2 or
H.sub.2 that react with the coke precursors or subdue or prevent
their formation during the methane aromatization reaction could be
added at levels of <10% vol. to the methane-containing feed to
improve the stability performance or regenerability of the
catalyst. The methane aromatization reaction is then carried out
until methane conversion falls to values that are lower than those
that are economically acceptable. At this point, the catalyst is
regenerated to restore its methane aromatization activity.
Following the regeneration, the catalyst is again contacted with a
methane-containing feed in a subsequent process cycle.
[0026] The catalyst regeneration can be performed by different
techniques known to those skilled in the art that are effective in
removing the carbonaceous deposits and restoring the catalyst
activity. For this particular invention, the spent catalysts were
regenerated by first cooling them from methane aromatization
reaction temperature to 480.degree. C. and then subjecting them to
purging with argon at 1000 h.sup.-1, atmospheric pressure and
480.degree. C. for one hour. Next, the catalysts were subjected to
2000 h.sup.-1 of 0.5 to 2.0% vol. O.sub.2/N.sub.2 gas flow at
atmospheric pressure and 480.degree. C. for 22 hrs to slowly burn
off the coke from their surface and restore their methane
aromatization activity.
EXAMPLES
[0027] The following Examples were carried out to compare the
catalytic performance of the methane aromatization catalyst of this
invention, prepared from molybdenum oxalate, with the catalysts
described in the prior art prepared from other (non-oxalate
containing) molybdenum precursors. The molybdenum precursor and
concentration level as well as the catalyst preparation method were
varied in these examples.
[0028] To remove any performance differences caused by the
inorganic oxide support, all catalysts described in the examples
were prepared using the same H-ZSM-5 zeolite support. The support
was prepared by calcining a batch of commercially available Zeolyst
International Company, CBV-3024E, NH.sub.4.sup.+/ZSM-5 zeolite
powder with SiO.sub.2/Al.sub.2O.sub.3 ratio of 30 under dry air at
500.degree. C. for a sufficient period of time to convert it from
NH.sub.4.sup.+ into H.sup.+ form.
[0029] The performance tests of all catalysts were conducted in the
same manner. Prior to testing, the catalysts were loaded into the
reactors as 2.5 cc charges and pretreated in situ by: (i)
establishing a 5 L/hr flow of pure H.sub.2, at 1 bar pressure and
heating from ambient temperature to 240.degree. C. at 0.5.degree.
C./min and holding at 240.degree. C. for 4 hrs; (ii) heating under
the same flow and pressure to 480.degree. C. at 2.degree. C./min
and holding at 480.degree. C. for 2 hrs and (iii) finally, heating
under the same conditions to 700.degree. C. at 2.degree. C./min and
holding at 700.degree. C. for at least 1.5 hours to complete the
reduction. The catalysts were purged with 2.5 L/hr of pure argon
for 20 min and then contacted with a methane-containing feed
comprising 90% vol. methane and 10% vol. argon at 1000 hr.sup.-1
GHSV, 1 bar pressure and 700.degree. C. The argon was used as an
internal standard for the GC analysis.
[0030] During the tests, full product samples were automatically
withdrawn from the reactor zone located directly under the catalyst
bed every 20 minutes and analyzed with a GC analyzer. The methane
conversion versus time on stream performance data obtained for all
catalysts (see Examples 1-20) is shown in FIG. 1. The figure shows
that the catalysts prepared from molybdenum oxalate precursor
(Examples 1-3), provide higher methane conversion than catalysts
prepared with other (non-oxalate) molybdenum precursors (Examples
4-20). The figure also shows that the molybdenum oxalate-derived
catalysts maintain their methane conversion better (exhibit better
stability) than the catalysts derived from non-oxalate
precursors.
[0031] FIG. 2 shows the corresponding benzene selectivity versus
methane conversion obtained in these tests. The data show, that the
catalysts prepared from a molybdenum oxalate precursor (Examples
1-3), provide higher benzene selectivity at higher methane
conversion than the catalysts prepared from non-oxalate precursors
(Examples 4-20). It should also be noted that, at the same
molybdenum loading level, the molybdenum oxalate-derived catalysts
exhibit higher methane conversion and higher benzene selectivity
and better stability relative to catalysts prepared using
non-oxalate precursors. This performance benefit was observed for
catalysts with very broad 4-15% wt of molybdenum loading. In
addition, among these catalysts, the 6-10% wt molybdenum containing
catalysts prepared from molybdenum oxalate precursors exhibited the
best combination of higher methane conversion, benzene selectivity
and performance stability relative to all other catalysts.
[0032] Following the above tests, the spent catalysts were
subjected to regeneration. The regeneration was carried out in situ
by first cooling the catalysts to 480.degree. C. and then purging
them with argon at 1000 h.sup.-1, 1 bar and 480.degree. C. for 1
hr. Next, the catalysts were subjected to 2000 h.sup.-1 of 0.5 to
2.0% vol. O.sub.2/N.sub.2 gas flow at atmospheric pressure and
480.degree. C. for 22 hrs to slowly burn off the coke from the
surface of the catalysts and restore their activity. The
regenerated catalysts were then subjected to performance
testing.
[0033] FIGS. 3 and 4 show the methane conversion versus time on
stream and benzene selectivity versus methane conversion test data,
respectively, for the regenerated catalysts. Again, the data show
that the regenerated catalysts prepared from molybdenum oxalate
precursors exhibit higher methane conversion and benzene
selectivity and higher stability relative to the regenerated
catalysts which were prepared from other molybdenum presursors.
[0034] The aforementioned catalysts were prepared as described in
the following Examples.
Example 1
[0035] A molybdenum oxalate solution was prepared by dissolving
144.07 g of MoO.sub.3 and 144.07 g of oxalic acid dihydrate (to
give a molar ratio of molybdenum to oxalic acid of 1:1.14) in a
1000 mL beaker filled with deionized water in such a way as to
prepare a total of 500 mL of 2 mol/L molybdenum oxalate solution.
The solution is then heated to 80.degree. C. and stirred for 4 hrs
or until complete dissolution of the molybdenum oxide and formation
of molybdenum oxalate.
[0036] Simultaneously, a sufficient quantity of NH4.sup.+-ZSM-5
zeolite powder was shaped by compacting it in a compactor at 250
bar and then sieved to obtain a support particles fraction of from
about 315-500 microns. The shaped NH4.sup.+ form zeolite support
particles were then placed in an oven and calcined at a temperature
of 500.degree. C. for 4 hours to convert them to an H.sup.+
form.
[0037] Eight grams of the H.sup.+-ZSM-5 zeolite support particles
were then impregnated with the molybdenum oxalate solution as
follows. The impregnation was carried out in a Perkin Elmer
MultiProbe II ex robotic pipetor that allows for automated
simultaneous impregnation of several support samples. First, the
impregnated support was weighed into a shallow bed dish and spread
evenly to maximize impregnation surface. The dish was then placed
in the Perkin Elmer Multiprobe in preparation for impregnation.
Next, a 2.66 mL quantity of the above described molybdenum oxalate
impregnation solution was mixed with 2.94 g of deionized water and
loaded in the pipetor. Then, the impregnation program was started
and the robotic head gradually impregnated the support in the dish
in reproducible manner.
[0038] The impregnated sample was then aged for 30 minutes; air
dried and then calcined in a programmable oven by subjecting it to
a 10 L/min flow of dry air and heating it to 300.degree. C. at a
rate of 1.degree. C. per minute. The temperature was maintained for
18 hours. Then, the temperature was raised to 550.degree. C. at a
rate of 1.degree. C. per minute and held for 2 hours. The calcined
catalyst sample was then sieved to remove fines and to obtain the
desired 315-500 microns fraction. The catalyst had a molybdenum
content of 6.0% wt.
Example 2
[0039] The catalyst of this example was prepared in the same manner
as the one in Example 1 except that 4.54 g (instead of 2.95 g) of
deionized water were added to the 2.66 mL solution of molybdenum
oxalate. In addition, the first step of the calcination of the
impregnated catalyst at 300.degree. C. was carried out for 2 hrs
instead of 18 hrs. The finished catalyst contained 6.0% wt of
molybdenum.
Example 3
[0040] The catalyst of this Example was prepared in the same manner
as the catalyst of Example 1. The only difference in this
preparation was the molybdenum loading. Specifically, 3.63 mL of
the molybdenum oxalate solution and 1.97 mL of deionized water we
used to prepare the impregnation solution and to achieve 8.0% w
molybdenum loading. The finished catalyst had a molybdenum content
of 8.0% wt.
Comparative Examples 4-20
Example 4
[0041] An ammoniumheptamolybdate solution was prepared by
dissolving 3.247 g of ammoniumheptamolybdate in 10 mL of deionized
water.
[0042] The zeolite support was prepared for impregnation following
the same steps as described Example 1. Ten grams of the zeolite
support, were impregnated with the aid of a pipette with 10 mL of
the ammoniumheptamolybdate solution. The impregnation was carried
out in a porcelain dish. Following the impregnation, the wet
zeolite support was manually mixed with a spatula, aged for 0.5 hrs
under shaking and then transferred to an oven for drying and
calcination. The drying was carried out by heating under air flow
of 1 L/min at a rate of 1.degree. C. per minute to 120.degree. C.
and holding at 120.degree. C. 10 hours. Then, the temperature was
raised to 500.degree. C. at a rate of 1.degree. C. per minute and
held for 6 hours. The finished catalyst sample was sieved to remove
fines and to obtain the desired 315-500 microns fraction. The
finished catalyst had a molybdenum content of 15.0% wt. It should
be noted that this sample was tested twice.
Example 5
[0043] The catalyst of this example was prepared in the same manner
as described in Example 4 except that the impregnating solution was
prepared by mixing 4.63 g of ammoniumheptamolybdate with 25 mL of
deionized water. Then, 5.07 mL of the above impregnation solution
was mixed with 2.13 g of deionized water and this final solution
was used to impregnate 8 g of zeolite support. Finally, a somewhat
different drying and calcining procedure was employed as described
below. The impregnated support was placed in a programmable oven
and dried and calcined in a 1 L/min flow of dry air by ramping the
temperature at a rate of 1.degree. C./min to 300.degree. C. and
holding for 2 hrs and then ramping the temperature at the same rate
to 550.degree. C. and holding for 2 hrs. The finished catalyst
sample was sieved to remove fines and to obtain the desired 315-500
microns fraction and then tested as described above. The catalyst
was found to have a molybdenum content of 6.0% wt.
Example 6
[0044] The catalyst of this example was prepared in a similar
manner as described in Example 5. In this case, an
ammoniumheptamolybdate solution was prepared by dissolving 4.63 g
of ammoniumheptamolybdate in 20 mL of water and adjusting the
volume to 25 mL to provide a solution with a molybdenum
concentration of 0.15 mol/L. Then, 11.03 mL of the above
impregnating solution was used to impregnate 10 g of the zeolite
support. The impregnated support was then placed in an oven and
dried with air (1 L/min) by heating to 70.degree. C. at a rate of
1.degree. C. per minute and holding for 10 hours. Then, the
temperature was increased to 120.degree. C. at a rate of 1.degree.
C. per minute and held for another 10 hours. Finally, the
temperature was increased to 500.degree. C. at a rate of 1.degree.
C. per minute and held for 5 hours. The finished catalyst sample
was sieved to remove fines and to obtain the desired 315-500
microns fraction and then tested as described above. The catalyst
was found to have a molybdenum content of 10.0% wt.
[0045] It should be noted that this particular catalyst was tested
twice.
Example 7
[0046] This example describes a methane aromatization catalyst
prepared by physical mixing or the so-called "solid state
ion-exchange" method. The zeolite support was prepared following
the same steps as described in the preceding examples. Then, 6.383
g of MoO.sub.3 powder were mixed with 100 g of the zeolite support.
The mixing was carried out by first dividing the 106.4 g mix into
ten separate 10.64 g portions. Next, the portions were mixed in a
grinder one portion at a time. The physical mixture was then
compacted in a Powtec compactor at a pressure force of 250 bar with
3 repetitions. The catalyst precursor was placed in a Microwave
furnace CEM and heated with nitrogen (1 L/min) at a temperature of
25.degree. C. for 4 hours. Then, the temperature was increased to
500.degree. C. at a rate of 25.degree. C. per minute and held for 2
more hours. The finished catalyst was sieved to remove fines and to
obtain the desired 315-500 microns fraction. The catalyst was found
to have a molybdenum content of 4.081% wt (equivalent to 6% wt of
MoO.sub.3).
Example 8
[0047] An impregnation solution was prepared by adding 28.08 g
MoO.sub.3 to 200 mL of deionized water and dissolving the oxide via
careful addition of NH.sub.4OH (25 wt %)until the pH of the
solution reached 9. The volume of the solution was then adjusted to
a total of 250 mL by addition of more deionized water. The zeolite
support was prepared for impregnation as described in the previous
examples. A final impregnation solution was prepared by mixing 9.0
mL of the above molybdenum solution (having pH=9) with 0.5 mL of
deionized water. The solution was then used to impregnate 10.5 g of
the zeolite support particles in the Perkin Elmer Multiprobe II ex
apparatus. The impregnation was accomplished as described in
Example 1. The impregnated zeolite support was then placed in a
programmable oven and dried and calcined under flow of dry air (1
L/min) by first increasing the temperature to 300.degree. C. at a
rate of 1.degree. C. per minute and holding for 1 hour. Next, the
temperature was increased to 550.degree. C. at a rate of 1.degree.
C. per minute and held for 2 hours. The finished catalyst was
sieved to remove fines and to obtain the desired 315-500 microns
fraction. The catalyst was found to have a molybdenum content of
6.0% wt.
Example 9
[0048] The catalyst of this example was prepared as described in
Example 7 except that 8.695 g MoO.sub.3 (8.0% wt.) were mixed with
100 g of the zeolite support. The support was calcined using a
conventional programmable oven rather than a microwave oven.
Specifically, the impregnated support was dried by placing it in
the oven and heating it at a rate of 1.degree. C./min in dry air (1
L/min) to 300.degree. C. and holding for 2 hours. Then the
temperature was increased to 550.degree. C. at a rate of 1.degree.
C. per minute and held for 2 hours. The finished catalyst was
sieved to remove fines and to obtain the desired 315-500 microns
fraction. The catalyst had a molybdenum content of 5.478% wt
(equivalent to 8 wt % MoO.sub.3).
Example 10
[0049] The catalyst of this Example was prepared in a similar
manner as described in Example 6. An ammoniumheptamolybdate
solution was prepared by dissolving 4.63 g of
ammoniumheptamolybdate in 20 mL of deionized water and adjusting
the volume to 25 mL to provide a solution with a molybdenum
concentration of 0.15 mol/L. The zeolite was subjected to
impregnation as a powder without shaping. The zeolite, 10 g, was
impregnated with a solution comprising 6.4 mL of the
ammoniumheptamolybdate solution and 2.7 mL of deionized water. The
zeolite powder and the solution were manually mixed with a spatula.
The impregnated support was dried and calcined by placing it in an
oven and heating it with dry air (1 L/min) at a rate of 1.degree.
C./min to 70.degree. C. and holding for 10 hours. Then the
temperature was increased to 120.degree. C. at a rate of 1.degree.
C. per minute and held for 10 hours. Finally, the temperature was
increased to 500.degree. C. at a rate of 1.degree. C. per minute
and held for 5 hours. The finished catalyst was sieved to remove
fines and to obtain the desired 315-500 microns fraction. The
catalyst had a molybdenum content of 6.0% wt.
Example 11
[0050] The catalyst of this example was prepared as described in
Example 5 except that the impregnation solution was prepared by
dissolving 3.09 g of ammoniumheptamolybdate in 25 mL of deionized
water. Also, 10 g of the zeolite support was impregnated with 9.5
mL of the above impregnating solution without further dilution. The
finished catalyst was sieved to remove fines and to obtain the
desired 315-500 microns fraction. The catalyst had a molybdenum
content of 6.0% wt.
Example 12
[0051] The catalyst was prepared as described in Example 5 but the
drying and calcination procedure followed was the one described in
Example 6. The finished catalyst was sieved to remove fines and to
obtain the desired 315-500 microns fraction. The catalyst had a
molybdenum content of 6.0% wt.
Example 13
[0052] An impregnating solution of molybdenum acetylacetonate was
prepared by adding 13.89 g of molybdenum acetylacetonate to 57.6 mL
of HNO.sub.3 (30% wt). The zeolite support was prepared for
impregnation as described in Example 1. The entire amount of
impregnating solution was then used to impregnate 64 g of the
zeolite support in a dish and then the impregnate was manually
mixed with a spatula as described in Example 4. The impregnated
zeolite was then dried and calcined under dry air flow of 1 L/min
by increasing the temperature at a rate of 1.degree. C./min to
300.degree. C. and holding for 2 hours. Then the temperature was
increased to 500.degree. C. at a rate of 1.degree. C. per minute
and held for 2 hours. The finished catalyst was sieved to remove
fines and to obtain the desired 315-500 microns fraction. The
catalyst had a molybdenum content of 6% wt.
Example 14
[0053] The catalyst of this Example was prepared in the same way as
described in Example 13 except that the final calcination
temperature was 550.degree. C. instead of 500.degree. C.
Example 15
[0054] The zeolite was used as a powder without shaping. The
zeolite was calcined at 500.degree. C. for 4 hours to convert it to
H.sup.+ form. Next, 5.746 g MoO.sub.3 (in solid form) was mixed
with 60 g of the zeolite powder in a mortar grinder. The molybdenum
oxide/zeolite mixture was then placed in a programmable oven and
calcined under dry air flow of 1 L/min by increasing the
temperature to 300.degree. C. at a rate of 1.degree. C. per minute.
The temperature was maintained for 2 hours. Then, the temperature
was increased to 550.degree. C. at a rate of 1.degree. C. per
minute and held for 2 hours. The finished catalyst sample was
sieved to remove fines and to obtain the desired 315-500 microns
fraction. The catalyst had a molybdenum content of 4.081% wt
(equivalent to 6% wt of MoO.sub.3).
Example 16
[0055] The catalyst of this Example was prepared in a similar
manner as the one of Example 5.
[0056] An ammoniumheptamolybdate solution was prepared by
dissolving 4.63 g of ammoniumheptamolybdate in 20 mL of deionized
water and adjusting the volume to 25 mL to provide a solution
having a molybdenum concentration of 0.15 mol/L.
[0057] The zeolite support was shaped and calcined as described in
Example 5. Then, 6.64 mL of the ammoniumheptamolybdate solution was
mixed with 2.66 g of deionized water to form the final impregnation
solution. The solution was used to impregnate 10 g of the zeolite
support. The freshly impregnated zeolite was manually mixed with a
spatula and aged for 0.5 hrs. The impregnated zeolite was then
dried and calcined using exactly the same procedure as described in
Example 6. The finished catalyst was sieved to remove the fines and
to obtain the desired 315-500 microns fraction. The catalyst had a
molybdenum content of 6% wt.
Example 17
[0058] The catalyst of this Example was prepared by the physical
mixing method. The zeolite powder was calcined at a temperature of
500.degree. C. for 4 hours to convert it to H.sup.+ form. Then,
0.8739 g MoO.sub.3 was mixed in a grinder with 10 g of the zeolite
powder. The mixture was then placed in a microwave furnace and kept
under nitrogen (1 L/min) at a temperature of 25.degree. C. for 4
hours. Then, the temperature was ramped at 25.degree. C./min to
500.degree. C. and held for 2 hours. Next, the catalyst was cooled,
mixed with 3% wt graphite and shaped into pellets with a 40 mm
diameter and 5 mm height. The pellets were crushed, sieved to
remove fines and obtain the desired 315-500 microns fraction for
testing. The catalyst had a molybdenum content of 5.504% wt.
Example 18
[0059] An ammoniumheptamolybdate solution was prepared by
dissolving 4.63 g of ammoniumheptamolybdate in 20 mL of deionized
water. The volume of the solutions was then adjusted to 25 mL with
deionized water to provide an impregnating solution with a
molybdenum concentration of 0.15 mol/L. The zeolite powder was
shaped by compacting it at 250 bar. The obtained zeolite support
was calcined at a temperature of 500.degree. C. for 4 hours. Then,
an impregnation solution comprising 6.34 mL of the above
ammoniumheptamolybdate solution and 2.66 g of deionized water was
prepared and used to impregnate 10 g of the zeolite support in a
porcelain dish. The freshly impregnated support was manually mixed
with a spatula and then aged for 0.5 hrs. Then, the impregnate was
placed in a programmable oven and dried under dry air (1 L/min) by
increasing the temperature from ambient to 70.degree. C. at a rate
of 1.degree. C. per minute and by holding at temperature for 10
hours. Then, the temperature was increased using the same rate to
120.degree. C. and held for another 10 hours. Finally, using the
same rate, the temperature was increased to 500.degree. C. and held
for 5 hours. The finished catalyst was sieved to remove the fines
and to obtain the desired 315-500 microns fraction. The catalyst
had a molybdenum content of 6% wt.
Example 19
[0060] The catalyst of this Example was prepared by the physical
mixture method. The zeolite powder was calcined at a temperature of
500.degree. C. for 4 hours to convert it to H.sup.+ form. Then,
0.6383 g MoO.sub.3 was mixed with 10 g of the zeolite powder in a
grinder. The obtained mixture was then placed in a microwave
furnace and heated under nitrogen (1 L/min) at a temperature of
25.degree. C. for 4 hours. Then, the temperature was increased at a
rate of 25.degree. C. per minute to 500.degree. C. and held for 2
hours. The catalyst was cooled, mixed with 3% wt graphite and
shaped into pellets with a 40 mm diameter and 5 mm height. The
catalyst was then crushed, sieved to remove fines and to obtain the
desired 315-500 microns fraction for testing. The catalyst had a
molybdenum content of 4.081% wt (equivalent to 6% wt of
MoO.sub.3).
Example 20
[0061] An ammoniumheptamolybdate solution was prepared by
dissolving 3.247 g of ammoniumheptamolybdate in 10 mL of deionized
water. Then, 10.0 mL of the ammoniumheptamolybdate solution was
used to impregnate 10 g of the zeolite powder. The impregnation was
done in a porcelain dish. Following the addition of the solution,
the mixture was mixed manually with the aid of a spatula and the
mix was aged for 0.5 hrs. The impregnated zeolite was then placed
in a programmable oven and dried and calcined under dry air (1
L/min) by increasing temperature from ambient to 120.degree. C.
using a heating rate of 1.degree. C. per minute and holding at
temperature for 10 hours. Then, using the same heating rate, the
temperature was increased to 500.degree. C. and held for 6 hours.
The finished catalyst was sieved to remove fines and to obtain the
desired 315-500 microns fraction. The catalyst had a molybdenum
content of 15% wt.
* * * * *