U.S. patent application number 10/317567 was filed with the patent office on 2004-06-17 for disproportionation of hydrocarbons.
Invention is credited to Johnson, Marvin M., Randolph, Bruce B., Sughrue, Edward L. II.
Application Number | 20040116764 10/317567 |
Document ID | / |
Family ID | 32506158 |
Filed Date | 2004-06-17 |
United States Patent
Application |
20040116764 |
Kind Code |
A1 |
Randolph, Bruce B. ; et
al. |
June 17, 2004 |
Disproportionation of hydrocarbons
Abstract
A novel hydrocarbon disproportionation process is provided and
includes contacting a hydrocarbon feed comprising at least one
paraffin with a disproportionation catalyst comprising a support
component, a metal, and a halogen in a disproportionation reaction
zone under disproportionation reaction conditions.
Inventors: |
Randolph, Bruce B.;
(Bartlesville, OK) ; Johnson, Marvin M.;
(Bartlesville, OK) ; Sughrue, Edward L. II;
(Bartlesville, OK) |
Correspondence
Address: |
RICHMOND, HITCHCOCK
FISH & DOLLAR
P.O. Box 2443
Bartlesville
OK
74005
US
|
Family ID: |
32506158 |
Appl. No.: |
10/317567 |
Filed: |
December 12, 2002 |
Current U.S.
Class: |
585/708 |
Current CPC
Class: |
C07C 2523/42 20130101;
C07C 2521/04 20130101; C07C 2523/75 20130101; C07C 2521/12
20130101; C07C 2521/02 20130101; C07C 2523/06 20130101; C07C
2523/08 20130101; C07C 2523/755 20130101; C07C 2523/46 20130101;
C07C 2521/06 20130101; C07C 2523/44 20130101; C07C 2527/06
20130101; C07C 6/10 20130101; C07C 2523/745 20130101; C07C 2529/04
20130101 |
Class at
Publication: |
585/708 |
International
Class: |
C07C 006/08 |
Claims
That which is claimed:
1. A process for disproportionating hydrocarbons comprising
contacting a hydrocarbon feed comprising at least one paraffin with
a catalyst comprising: (a) a support component, (b) a metal
selected from the group consisting of platinum, palladium, iron,
cobalt, nickel, zinc, ruthenium, rhodium, osmium, iridium, and
combinations of any two or more thereof, and (c) a halogen in a
disproportionation reaction zone under disproportionation reaction
conditions.
2. A process in accordance with claim 1 further comprising
reactivating said catalyst by stripping said catalyst with
hydrogen.
3. A process in accordance with claim 1 wherein said hydrocarbon
feed further comprises an initiator selected from the group
consisting of a chloroalkane, a branched paraffin, at least one
olefin, and combinations of any two or more thereof.
4. A process in accordance with claim 3 wherein the concentration
of said initiator in said disproportionation reaction zone, based
on the combined weight of said hydrocarbon feed and said initiator
in said reaction zone, is at least about 0.01 weight percent.
5. A process in accordance with claim 3 wherein the concentration
of said initiator compound in said reaction zone, based on the
combined weight of said hydrocarbon feed and said initiator in said
reaction zone, is at least about 0.1 weight percent.
6. A process in accordance with claim 3 wherein the concentration
of said initiator in said reaction zone, based on the combined
weight of said hydrocarbon feed and said initiator in said reaction
zone, is at least 0.9 weight percent.
7. A process in accordance with claim 3 wherein said at least one
olefin has in the range of from 2 to 20 carbon atoms per
molecule.
8. A process in accordance with claim 3 wherein said at least one
olefin has in the range of from 3 to 8 carbon atoms per
molecule.
9. A process in accordance with claim 3 wherein said at least one
olefin has in the range of from 5 to 6 carbon atoms per
molecule.
10. A process in accordance with claim 1 wherein said
disproportionation reaction conditions include a temperature in the
range of from about 75.degree. F. to about 500.degree. F.
11. A process in accordance with claim 1 wherein said
disproportionation reaction conditions include a temperature in the
range of from about 100.degree. F. to about 300.degree. F.
12. A process in accordance with claim 1 wherein said
disproportionation reaction conditions include a temperature in the
range of from 200.degree. F. to 300.degree. F.
13. A process in accordance with claim 1 wherein said metal of said
catalyst is selected from the group consisting of platinum,
palladium, and combinations thereof.
14. A process in accordance with claim 1 wherein said halogen of
said catalyst is selected from the group consisting of chlorine,
bromine and combinations thereof.
15. A process in accordance with claim 1 wherein said support
component of said catalyst is selected from the group consisting of
alumina, silica-alumina, a zeolite, zirconia, a borate, an aluminum
borate, and combinations thereof.
16. A process in accordance with claim 1 wherein said metal of said
catalyst comprises platinum, said halogen of said catalyst
comprises chlorine, and said support component of said catalyst
comprises alumina.
17. A process in accordance with claim 1 wherein said catalyst
further comprises an element selected from the group consisting of
boron, gallium, indium, thallium, and combinations of any two or
more thereof.
18. A process in accordance with claim 17 wherein said element
comprises gallium.
Description
[0001] This invention relates to the disproportionation of
hydrocarbons. More particularly, this invention relates to the
disproportionation of paraffins in the presence of an isomerization
catalyst.
BACKGROUND OF THE INVENTION
[0002] The disproportionation of hydrocarbons is well known in the
art. This process has gained importance due to governmental
regulations requiring reduction of the amount of volatile C.sub.4
and C.sub.5 alkanes present in gasoline. Also, there is an
incentive to convert isopentanes, for example, to higher
isoparaffins, such as, isohexane which is a lower vapor pressure
motor fuel component, and to isobutane which is a feedstock for
alkylation with olefins to high octane alkylate and also for the
production of MTBE.
[0003] Therefore, development of an improved process for
disproportionating hydrocarbons would be a significant contribution
to the art.
SUMMARY OF THE INVENTION
[0004] It is an object of the present invention to provide an
improved process for disproportionating hydrocarbons.
[0005] It is another object of the present invention to provide an
improved process for disproportionating hydrocarbons by contacting
a hydrocarbon feedstock with a catalyst comprising a metal, a
halogen, and a support component.
[0006] In accordance with the present invention, a process for
disproportionating hydrocarbons has been discovered comprising
contacting a hydrocarbon feed comprising at least one paraffin with
a catalyst comprising a support component, a metal, and a halogen
in a disproportionation reaction zone under disproportionation
reaction conditions.
[0007] Other objects and advantages will become apparent from the
detailed description and the appended claims.
DETAILED DESCRIPTION OF THE INVENTION
[0008] The process of the present invention comprises, consists of,
or consists essentially of contacting a hydrocarbon feed comprising
at least one paraffin with a catalyst comprising
[0009] (a) a support component,
[0010] (b) a metal selected from the group consisting of platinum,
palladium, iron, cobalt, nickel, zinc, ruthenium, rhodium, osmium,
iridium, and combinations of any two or more thereof, and
[0011] (c) a halogen in a disproportionation reaction zone under
disproportionation reaction conditions.
[0012] The hydrocarbon feed can be any hydrocarbon-containing feed
which comprises, consists of, or consists essentially of at least
one paraffin. Preferably, the feed comprises at least one C.sub.4
or C.sub.5 paraffin including, but not limited to, normal butane,
normal pentane, and isopentane. Most preferably, the feed comprises
at least one isopentane.
[0013] The hydrocarbon feed can be a stream obtained from an
alkylation process, or obtained from the processing of natural gas
liquids, or a stream obtained from a thermal or catalytic cracking
process.
[0014] The catalyst used in the inventive process can comprise,
consist of, or consist essentially of (a) a support component, (b)
a metal selected from the group consisting of platinum, palladium,
iron, cobalt, nickel, zinc, ruthenium, rhodium, osmium, iridium,
and combinations of any two or more thereof, and (c) a halogen.
Preferably, the halogen is selected from the group consisting of
chlorine, bromine, and combinations thereof, and the metal is
selected from the group consisting of platinum, palladium, and
combinations thereof, and the support component is selected from
the group consisting of alumina, silica-alumina, a zeolite,
zirconia, a borate, an aluminum borate, and combinations thereof.
Most preferably, the support component comprises alumina, the metal
comprises platinum, and the halogen comprises chlorine.
[0015] The process of this invention preferably employs an
initiator, which is added to the hydrocarbon feed. The initiator is
selected from the group consisting of a chloroalkane, a branched
paraffin, at least one olefin, and combinations thereof.
Preferably, the initiator comprises at least one olefin.
[0016] The initiator useful in the present invention can be any
compound capable of initiating a hydrogen transfer reaction. The
chloroalkane preferably comprises a compound selected from the
group consisting of chloropropane, chlorobutanes, chloropentanes,
and combinations of any two or more thereof. The branched paraffin
preferably comprises a multi-branched paraffin having a different
molecular weight than the primary component in the hydrocarbon
feed. The at least one olefin preferably has in the range of from 2
to 20 carbon atoms per molecule, and combinations of any two or
more thereof. More preferably, the at least one olefin has in the
range of from 3 to 8 carbon atoms per molecule. Most preferably,
the at least one olefin has in the range of from 5 to 6 carbon
atoms per molecule.
[0017] When present, the concentration of the initiator in the
disproportionation reaction zone, based on the combined weight of
the hydrocarbon feed and initiator in the disproportionation
reaction zone, is at least about 0.01 weight percent, preferably at
least about 0.1 weight percent and most preferably at least 0.9
weight percent.
[0018] In another embodiment of the invention, the catalyst
comprises, consists of, or consists essentially of a) a support
component, b) a metal selected from the group consisting of
platinum, palladium, iron, cobalt, nickel, zinc, ruthenium,
rhodium, osmium, iridium, and combinations of any two or more
thereof, c) a halogen and d) an element selected from the group
consisting of boron, gallium, indium, thallium, and combinations of
any two or more thereof Preferably, the element is gallium.
[0019] The disproportionation reaction takes place in a
disproportionation reaction zone. The disproportionation reaction
zone can be any reactor system known to those skilled in the art to
be suitable for use in disproportionating hydrocarbons in the
presence of a catalyst. Typical reactor systems useful in the
present invention include, but are not limited to, batch type
operations, a fixed bed system, a moving bed system, and a
fluidized bed system.
[0020] The disproportionation reaction conditions can be any
conditions suitable for disproportionating hydrocarbons.
Preferably, the disproportionation reaction conditions include a
temperature in the range of from about 75.degree. F. to about
500.degree. F., more preferably from about 100.degree. F. to about
300.degree. F., and most preferably from 200.degree. F. to
300.degree. F. Also, the disproportionation reaction conditions
include a contact time of the hydrocarbon feed with the
disproportionation catalyst in the range of from about 30 seconds
to about 2 hours, preferably from about 5 minutes to about 1 hour,
and most preferably from 20 minutes to 50 minutes, and, optionally,
include the presence of the above described initiator.
[0021] The catalyst can be reactivated by being stripped with
hydrogen.
[0022] The following examples demonstrate the advantages of the
present invention. The examples are for illustration purposes only
and are not intended to limit the invention as set out in the
specification and the appended claims.
EXAMPLE I
[0023] A 20 mL sample of a catalyst containing 1.5% Ga.sub.2O.sub.3
on Al.sub.2O.sub.3 with 0.3% platinum was placed into a tubular
reactor with an inert support above and below the catalyst. A
nitrogen feed was set at 50 sccm and the temperature was set at
500.degree. F. A 3.4 gram quantity of carbon tetrachloride was
charged to the reactor at a rate of 0.1 mL/min. After this catalyst
was chlorided, as described above, an isopentane feed was charged
to the reactor at a feed rate of 42.4 mL/hr (LHSV=2 hr.sup.-1).
Initial temperature was set at 250.degree. F. and a hydrogen
co-feed was set at 2.5 sccm. Table I shows the results for five
different samples taken approximately after 1 hour, 2 hours, 3
hours, 4.5 hours and 5.5 hours on stream, respectively.
1TABLE I iC.sub.5 Disproportionation Results from Platinum on
Chlorided Alumina Catalyst with Gallium Time On-Stream, Hours Feed
1 Hour 2 Hours 3 Hours 4.5 Hours 5.5 Hours Product (wt %) propane 0
0.089 0.007 0.004 0.002 0.001 isobutane 0.053 10.932 3.100 1.778
0.903 0.636 butene 0 0.002 0 0.001 0 0 normal butane 0.084 0.406
0.105 0.100 0.091 0.088 neo-pentane 0.193 0.209 0.19456 0.194 0.193
0.193 isopentane 99.235 78.384 91.126 94.155 96.690 97.444 normal
pentane 0.414 1.580 0.892 0.757 0.652 0.634 Unknown C.sub.1-C.sub.5
0.021 0.017 0.021 0.020 0.020 0.019 2,2-dimethylbutane 0 0.254
0.042 0.035 0.02 0.010 2,3-dimethylbutane 0 0.879 0.413 0.257 0.116
0.083 2-methylpentane 0 3.602 2.026 1.354 0.663 0.475
3-methylpentane 0 1.805 1.11 0.758 0.377 0.276 normal hexane 0
0.256 0.086 0.047 0.018 0.012 Unknown C.sub.6 0 0.004 0 0 0 0
2,2-dimethylpentane 0 0.018 0.004 0.002 0.001 0 2,4-dimethylpentane
0 0.182 0.074 0.044 0.016 0.008 2,2,3-trimethylbutane 0 0.035 0.011
0.007 0.003 0.001 3,3-dimethylpentane 0 0.037 0.038 0.007 0.010
0.003 2-methylhexane 0 0.36 0.17 0.102 0.037 0.018
2,3-dimethylpentane 0 0.115 0.055 0.033 0.012 0.006 3-methylhexane
0 0.282 0.142 0.084 0.030 0.015 3-ethylpentane 0 0.014 0.008 0.004
0.001 0 2,2,4-trimethylpentane 0 0.003 0 0 0 0 normal C.sub.7 0
0.044 0.018 0.010 0.004 0.002 Unknown C.sub.7 0 0.023 0.008 0.006
0.004 0.002 2,2-dimethylhexane 0 0.014 0.006 0.004 0.002 0.001
2,5-dimethylhexane 0 0.038 0.017 0.011 0.005 0.002
2,4-dimethylhexane 0 0.037 0.018 0.011 0.005 0.002
3,3-dimethylhexane 0 0.004 0.001 0.001 0 0 2,3,4-trimethylpentane 0
0.002 0 0 0 0 2,3,3-trimethylpentane 0 0.001 0 0 0 0
2,3-dimethylhexane 0 0.012 0.006 0.004 0.002 0 2-methylheptane 0
0.044 0.023 0.015 0.006 0.002 4-methylheptane 0 0.013 0.007 0.004
0.002 0 3,4-dimethylhexane 0 0.004 0.002 0.001 0 0 3-methylheptane
0 0.040 0.022 0.014 0.006 0.002 Unknown C.sub.8 0 0.001 0.001 0.001
0.001 0.001 C.sub.9.sup.+ 0 0.254 0.244 0.172 0.108 0.064
[0024] The catalyst underwent hydrogen stripping for 65 hours at a
hydrogen flow rate of 50 sccm with temperature set at 300.degree.
F. After reactivation, an isopentane feed was once again charged to
the reactor at a feed rate of 42.4 mL/hr (LHSV=2 hr.sup.-1).
Initial temperature was set at 270.degree. F. and a hydrogen
co-feed was set at 2.5 sccm. Table II shows the results for 5
different samples taken approximately 1, 2, 3, 4 and 5 hours after
reactivation, respectively.
2TABLE II iC.sub.5 Disproportionation Results from Platinum on
Chlorided Alumina Catalyst with Gallium Time Since Reactivation,
Hours Feed 1 Hour 2 Hours 3 Hours 4 Hours 5 Hours Product (wt %)
Propane 0 0.058 0.010 0.005 0.003 0.006 Isobutane 0.053 9.389 4.350
2.754 1.946 2.378 Butene 0 0.002 0.001 0 0.001 0.001 normal butane
0.084 0.265 0.109 0.097 0.093 0.097 neo-pentane 0.193 0.202 0.195
0.194 0.194 0.194 Isopentane 99.235 79.064 88.199 91.422 93.854
93.051 normal pentane 0.414 2.313 1.383 1.187 1.094 1.214 Unknown
C.sub.1-C.sub.5 0.021 0.020 0.022 0.022 0.024 0.021
2,2-dimethylbutane 0 0.178 0.066 0.036 0.021 0.044
2,3-dimethylbutane 0 0.098 0.594 0.433 0.277 0.324 2-methylpentane
0 3.794 2.618 2.019 1.36 1.45 3-methylpentane 0 2.083 1.456 1.129
0.767 0.809 normal hexane 0 0.339 0.163 0.104 0.060 0.092 Unknown
C.sub.6 0 0.002 0 0 0 0 2,2-dimethylpentane 0 0.014 0.005 0.003
0.001 0.002 2,4-dimethylpentane 0 0.159 0.094 0.063 0.028 0.036
2,2,3-trimethylbutane 0 0.034 0.016 0.010 0.004 0.007
3,3-dimethylpentane 0 0.020 0.009 0.006 0.002 0.004 2-methylhexane
0 0.348 0.217 0.146 0.069 0.080 2,3-dimethylpentane 0 0.124 0.074
0.049 0.022 0.028 3-methylhexane 0 0.297 0.185 0.124 0.059 0.668
3-ethylpentane 0 0.017 0.010 0.007 0.003 0.004
2,2,4-trimethylpentane 0 0 0 0 0 0 normal C.sub.7 0 0.054 0.028
0.019 0.008 0.011 Unknown C.sub.7 0 0 0 0 0 0 2,2-dimethylhexane 0
0.012 0.01 0.005 0.003 0.002 2,5-dimethylhexane 0 0.024 0.016 0.011
0.005 0.004 2,4-dimethylhexane 0 0.027 0.175 0.012 0.005 0.004
3,3-dimethylhexane 0 0.002 0.002 0.001 0 0 2,3-dimethylhexane 0
0.01 0.006 0.004 0.002 0.002 2-methylheptane 0 0.033 0.022 0.016
0.007 0.006 4-methylheptane 0 0.011 0.007 0.005 0.002 0.002
3,4-dimethylhexane 0 0.004 0.002 0.002 0 0 3-methylheptane 0 0.033
0.022 0.016 0.007 0.006 Unknown C.sub.8 0 0.002 0.001 0.001 0.001 0
C.sub.9.sup.+ 0 0.009 0.091 0.09 0.075 0.057
[0025] The catalyst was once again reactivated. After reactivation
an isopentane feed was charged to the reactor at a feed rate of
21.2 mL/hr (LHSV=1 hr.sup.-1). Initial temperature was set at
270.degree. F. and a hydrogen co-feed was set at 2.5 sccm. Table
III shows the results for five different samples taken
approximately two hours, three hours, four hours, five hours, and
six hours after reactivation, respectively.
3TABLE III iC.sub.5 Disproportionation Results from Platinum on
Chlorided Alumina Catalyst with Gallium Time Since Reactivation,
Hours Feed 2 Hour 3 Hours 4 Hours 5 Hours 6 Hours Product (wt %)
ethane 0 0 0.008 0.001 0.001 0.002 propane 0 0.049 0.020 0.014
0.013 0.018 isobutane 0.053 9.501 7.692 6.262 6.127 6.967 butene 0
0.001 0.001 0.001 0.001 0.001 normal butane 0.084 0.225 0.131 0.118
0.117 0.125 neo-pentane 0.193 0.201 0.193 0.194 0.194 0.194
isopentane 99.235 77.846 79.659 82.890 83.390 81.726 normal pentane
0.414 2.243 1.975 1.748 1.728 1.697 Unknown C.sub.1-C.sub.5 0.021
0.015 0.021 0.024 0.026 0.028 2,2-dimethylbutane 0 0.149 0.101
0.073 0.071 0.086 2,3-dimethylbutane 0 1.148 1.179 0.991 0.945
1.031 2-methylpentane 0 4.346 4.593 4.012 3.895 4.204
3-methylpentane 0 2.385 2.525 2.195 2.128 2.289 normal hexane 0
0.349 0.303 0.229 0.217 0.248 Unknown C.sub.6 0 0.004 0.002 0 0.002
0.002 2,2-dimethylpentane 0 0.013 0.007 0.005 0.004 0.006
2,4-dimethylpentane 0 0.18 0.190 0.146 0.132 0.161
2,2,3-trimethylbutane 0 0.037 0.032 0.023 0.020 0.026
3,3-dimethylpentane 0 0.019 0.014 0.010 0.009 0.012 2-methylhexane
0 0.404 0.429 0.333 0.306 0.367 2,3-dimethylpentane 0 0.145 0.151
0.116 0.105 0.127 3-methylhexane 0 0.346 0.367 0.283 0.260 0.311
3-ethylpentane 0 0.020 0.020 0.016 0.014 0.017 Normal C.sub.7 0
0.059 0.052 0.038 0.032 0.041 2,2-dimethylhexane 0 0.014 0.012
0.009 0.008 0.010 2,5-dimethylhexane 0 0.030 0.032 0.024 0.022
0.027 2,4-dimethylhexane 0 0.033 0.035 0.027 0.024 0.030
3,3-dimethylhexane 0 0.003 0.002 0.002 0.002 0.002
2,3-dimethylhexane 0 0.012 0.013 0.010 0.009 0.011 2-methylheptane
0 0.042 0.045 0.034 0.031 0.038 4-methylheptane 0 0.014 0.015 0.011
0.010 0.013 3,4-dimethylhexane 0 0.004 0.005 0.004 0.003 0.004
3-methylheptane 0 0.042 0.045 0.034 0.031 0.038 Unknown C.sub.8 0
0.005 0.004 0.004 0.004 0.005 C.sub.9.sup.+ 0 0.112 0.123 0.117
0.118 0.131
[0026] As is evident from the results, the catalyst can still
convert isopentane even after two reactivations.
EXAMPLE II
[0027] An 11 mL sample of a catalyst containing 18% gallium in a
mixed (Ga/Al).sub.2O.sub.3 support with 0.5% platinum was placed
into a tubular reactor with an inert support above and below the
catalyst. A nitrogen feed was set at 50 sccm and the temperature
was set at 500.degree. F. A 2.52 gram quantity of carbon
tetrachloride was charged to the reactor at a rate of 0.035 mL/min.
After this catalyst was chlorided, as described above, a pure
isopentane feed was charged to the reactor at a feed rate of 22
mL/hr (LHSV=2 hr.sup.-1). The initial pressure was set at 300 psig.
Initial temperature was set at 235.degree. F. and a hydrogen
co-feed was set at 2.5 sccm. Table IV shows the results for five
different samples taken approximately after 1, 2, 3, 4 and 5 hours
on stream, respectively.
4TABLE IV iC.sub.5 Disproportionation Results from Platinum on
Chlorided Alumina Catalyst with Gallium Time On-Stream, Hours 1
Hour 2 Hours 3 Hours 4 Hours 5 Hours Total Product (wt %) Propane
0.03 0.01 0.01 0.00 0.00 Isobutene 14.18 5.27 5.13 2.63 1.64
Isobutene 0.00 0.00 0.00 0.00 0.00 Normal Butane 0.22 0.11 0.12
0.09 0.09 Neo-pentane 0.22 0.21 0.20 0.21 0.22 Isopentane 57.40
81.26 81.79 91.35 94.13 Normal Pentane 1.92 1.46 1.45 1.02 1.03
Unknown C.sub.1-C.sub.5 0.05 0.04 0.03 0.02 0.02 2,2-dimethylbutane
0.84 0.29 0.32 0.08 0.03 2,3-dimethylbutane 2.27 1.14 1.03 0.45
0.28 2-methylpentane 7.02 4.07 3.77 1.91 1.34 3-methylpentane 3.17
1.86 1.80 0.93 0.67 Normal Hexane 0.38 0.14 0.14 0.05 0.03
C.sub.7.sup.+ 12.30 4.13 4.22 1.25 0.54 Total C.sub.6.sup.+ 25.98
11.63 11.28 4.66 2.88 C.sub.6 Selectivity 52.7 64.5 62.5 73.3
81.2
[0028] As is evident from the results, the catalyst as prepared in
Example II is also useful for converting isopentane.
[0029] The pressure was then decreased to 25 psig. The hydrogen
co-feed was set at 5 sccm. Table V shows the results for three
different samples taken after approximately 6 hours, 8 hours, and
10 hours on stream, respectively.
5TABLE V i-C.sub.5 Disproporationation Results from Platinum on
Chlorided Alumina Catalyst with Gallium Time on Stream Hours 6
Hours 8 Hours 10 Hours Liquid Product (wt %) Propane 0.001 0 0
Isobutane 0.356 0.257 0.285 Normal Butane 0.078 0.079 0.082
Neo-pentane 0.204 0.208 0.212 Isopentane 95.494 98.200 98.503
Normal Pentane 0.42 0.428 0.432 2,2-dimethylbutane 0.001 0 0
2,3-dimethylbutane 0.046 0.031 0.028 2-methylpentane 0.308 0.233
0.224 3-methylpentane 0.187 0.135 0.130 Normal Hexane 0.002 0.001
0.001 C.sub.7.sup.+ 2.902 0.429 0.103 Offgas (wt %) Propane 0.304
0.136 0.066 Isobutane 12.401 6.403 3.651 Normal Butane 0.292 0.243
0.232 Neo-pentane 0 0.332 0.377 Isopentane 72.047 83.163 90.403
Normal Pentane 1.075 0.529 0.400 2,2-dimethylbutane 0 0.063 0.035
2,3-dimethylbutane 0.616 0.254 0.125 2-methylpentane 2.022 0.798
0.410 3-methylpentane 1.095 0.352 0.190 Normal Hexane 0 0.068 0.034
C.sub.7.sup.+ 10.149 7.659 4.075 Combined (wt %) Propane 0.128
0.028 0.010 Isobutane 5.423 1.525 0.781 Normal Butane 0.168 0.113
0.104 Neo-pentane 0.118 0.234 0.236 Isopentane 85.630 95.098 97.309
Normal Pentane 0.696 0.448 0.427 2,2-dimethylbutane 0.001 0.013
0.005 2,3-dimethylbutane 0.286 0.077 0.042 2-methylpentane 1.029
0.349 0.251 3-methylpentane 0.569 0.179 0.139 Normal Hexane 0.001
0.015 0.006 C.sub.7.sup.+ 5.951 1.920 0.689 Isopentane Conversion
14.5% 4.0% 2.5%
[0030] As is evident from Table V, the catalyst as prepared in
Example II can also convert isopentane after being reactivated.
[0031] Whereas this invention has been described in terms of the
preferred embodiments, reasonable variations and modifications are
possible by those skilled in the art. Such modifications are within
the scope of the described invention and appended claims.
* * * * *