U.S. patent application number 11/113993 was filed with the patent office on 2005-11-24 for process for production of high-octane gasoline.
Invention is credited to Houzvicka, Jindrich.
Application Number | 20050258076 11/113993 |
Document ID | / |
Family ID | 34934967 |
Filed Date | 2005-11-24 |
United States Patent
Application |
20050258076 |
Kind Code |
A1 |
Houzvicka, Jindrich |
November 24, 2005 |
Process for production of high-octane gasoline
Abstract
The invention provides a process for production of high-octane
gasoline from a C.sub.6-C.sub.10 hydrocarbon feed stream by
selective dehydrogenation of cycloparaffins without substantially
affecting aromatics and paraffins present in the feed. It involves
a catalyst comprising a Group VIII metal supported on a
substantially non-acidic porous material with concentration of
acidic sites lower than 1 .mu.mole/g. The catalyst in the selective
dehydrogenation typically comprises palladium, platinum, rhodium,
iridium or mixtures thereof in an amount of 0.1 wt % to 1.0 wt %
supported on a carrier material selected from silica, alumina,
zirconia, titania, or mixtures thereof, other oxides, carbons,
carbides and nitrides. The process for the production of
high-octane gasoline from a C.sub.6-C.sub.10 hydrocarbon feed can
be a combination of a catalytic dehydrogenation step, a catalytic
isomerisation step and one or more separation steps.
Inventors: |
Houzvicka, Jindrich;
(Turnov, CZ) |
Correspondence
Address: |
DICKSTEIN SHAPIRO MORIN & OSHINSKY LLP
2101 L Street, NW
Washington
DC
20037
US
|
Family ID: |
34934967 |
Appl. No.: |
11/113993 |
Filed: |
April 26, 2005 |
Current U.S.
Class: |
208/134 ;
208/137; 208/62 |
Current CPC
Class: |
C10G 35/085 20130101;
C10G 59/02 20130101; B01J 23/464 20130101; B01J 23/44 20130101;
B01J 23/58 20130101; B01J 37/0201 20130101 |
Class at
Publication: |
208/134 ;
208/137; 208/062 |
International
Class: |
C10G 035/04; C10G
059/02 |
Foreign Application Data
Date |
Code |
Application Number |
May 18, 2004 |
DK |
PA 2004 00795 |
Claims
1. A process for production of high-octane gasoline from a
C.sub.6-C.sub.10 hydrocarbon feed stream comprising the step of
selective dehydrogenation of cycloparaffins, wherein the
dehydrogenation takes place in presence of a catalyst comprising
one or more Group VIII metal supported on a porous material with
concentration of acidic sites lower than 1 .mu.mole/g.
2. A process according to claim 1, wherein the catalyst in the
dehydrogenation step comprises palladium, platinum, rhodium,
iridium or mixtures thereof in an amount of 0.1 wt % to 1.0 wt %
supported on a carrier material selected from silica, alumina,
zirconia, titania, or mixtures thereof, other oxides, carbons,
carbides and nitrides.
3. A process according to claim 1, wherein the dehydrogenation step
is performed at temperatures between 350.degree. C. and 550.degree.
C., in presence of hydrogen, at a total pressure between 5 to 50
bar and with a hydrogen to hydrocarbon molar ratio between 1 to
5.
4. A process according to claim 1, comprising further steps of
catalytic isomerization step converting linear and mono-branched
isomers to multi-branched paraffins and/or cyclo-pentane derivates
to cyclo-hexane derivates, and separation step separating aromatic
compounds and multi-branched isomers from non-converted
cyclo-alkanes, linear and mono-branched paraffins.
5. A process according to claim 4, wherein the catalyst in the
isomerisation step comprises an acidic mesoporous material.
6. A process according to claim 5, wherein the mesoporous material
comprises tungsten oxide supported on zirconia, titania, alumina,
silica, hafnia or tin oxide or mixture thereof with tungsten
content between 5 wt % to 50 wt % and palladium, platinum or
mixtures thereof with a loading 0.01 wt % to 2 wt %.
7. A process according to claim 4, wherein the isomerisation step
is performed in the presence of hydrogen with a hydrogen to
hydrocarbon molar ratio between 0.1 to 5, in the temperature range
150.degree. C. to 300.degree. C., at a total pressure between 1 and
40 bar and with a liquid space velocity LHSV between 0.1 to 30
h.sup.-1.
8. A process according to claim 4, wherein the non-converted
cyclo-alkanes, the linear and the mono-branched paraffins are
separated from the multi-branched paraffins and the aromatic
compounds and said non-converted cyclo-alkanes and linear and
mono-branched paraffins are recycled to the isomerisation or to the
dehydrogenation step.
Description
BACKGROUND OF THE INVENTION
[0001] 1. Field of the Invention
[0002] The invention relates to a process for upgrading a
C.sub.6-C.sub.10 paraffin/cycloparaffin refinery stream.
[0003] The invention is specifically directed to a process for
selective dehydrogenation of C.sub.6-C.sub.10 cycloparaffins in
presence of C.sub.6-C.sub.10 paraffins and aromatics for use in
high octane gasoline.
[0004] 2. Description of Related Art
[0005] The C.sub.6-C.sub.10 fraction of crude oil consists
basically of three main groups of components: aromatics, linear or
mono-branched paraffins and cycloparaffins. While aromatics are
valuable gasoline blending components due to their high octane
numbers, the octane numbers of the components in the other groups
are too low to be used without upgrading.
[0006] A process for upgrading gasoline-type hydrocarbon mixtures
to fuels having a higher octane rating is disclosed in U.S. Pat.
No. 4,644,089, where alkanes and cyclo-alkanes are converted to
alkenes, aromatics and hydrogen in presence of a catalyst, which
comprises vanadium oxide and aluminum phosphate. However, alkenes
are not desired components of a high octane gasoline, further, the
catalyst deactivates and a reactivation process is disclosed as
well.
[0007] In U.S. Pat. No. 6,338,791 a process for producing high
octane number gasoline is described. The process is a
hydroisomerisation of C.sub.5-C.sub.8 cuts comprising paraffinic,
naphthenic, aromatic and olefinic hydrocarbons followed by at least
one separation and a recycling of low octane number paraffins. The
process converts straight chain paraffins to branched paraffins,
however, nothing is mentioned about cycloalkanes.
[0008] In the description of U.S. Pat. No. 4,607,129, a catalytic
conversion of alkanes up to C.sub.20 is disclosed, which upgrades a
gasoline type hydrocarbon mixture. The catalyst comprises vanadium
oxides and silica, and it converts cycloalkanes and cycloalkenes
and aromatic hydrocarbons by reforming. However, alkenes do not
increase octane number of gasoline.
[0009] A catalyst for conversion of hydrocarbons into aromatics is
described in U.S. Pat. No. 6,007,700, where the conversion is a
reforming process and the catalyst comprises alumina, a doping
metal, a noble metal, a promoter metal and a halogen. By this
method, hydrocarbons are converted into aromatics, however, some
cracking also occurs.
[0010] EP 1 233 050 discloses a process for upgrading naphtha by
increasing the content of aromatics. The process involves
dehydrogenation of paraffins to olefins and further dehydrogenation
of cycloparaffins in this mixture to aromatic compounds. The aim of
this process is to create aromatics, the catalyst, which is used
for the aromatization, is a catalyst on a refractory support, which
provides acid sites for cracking, isomerization and
cyclozation.
[0011] This means that C.sub.6-C.sub.10 fraction is currently
mostly processed by catalytic reforming, where majority of the feed
is converted to aromatics. There are three disadvantages of this
solution. First, aromatics are very health-hazardous compounds and
their maximum content is under legislation pressure. Second,
aromatics are the densest compounds out of the three groups.
Aromatisation of paraffins and cycloparaffins results in a
significant volumetric shrinkage of up to 25%, which decreases
economic benefit of the process. Third, volumetric yield is further
decreased by low selectivity of aromatisation of shorter paraffins.
C.sub.6 paraffins in particular tend to crack to gas under the
reaction conditions used in the reforming process.
[0012] Due to economy reasons, the most efficient solution would be
to up-grade only cycloparaffins to aromatics, while the paraffinic
fraction is converted by isomerisation to multi-branched isomers.
However, paraffins are very susceptible to cracking under the
typical conditions during such reactions at elevated
temperatures.
[0013] It has now been found that process conditions and catalyst
subjected to this invention allow selective dehydrogenation of
cycloparaffins in presence of branched paraffins without their
dehydrogenation or cracking to gas.
SUMMARY OF THE INVENTION
[0014] The invention provides a process for production of
high-octane gasoline from a C.sub.6-C.sub.10 hydrocarbon feed
stream by selective dehydrogenation of cycloparaffins without
substantially affecting aromatics and paraffins present in the
feed. It involves a catalyst comprising a Group VIII metal
supported on a substantially non-acidic porous material with
concentration of acidic sites lower than 1 .mu.mole/g.
[0015] The catalyst in the selective dehydrogenation typically
comprises palladium, platinum, rhodium, iridium or mixtures thereof
in an amount of 0.1 to 1.0 wt % supported on a carrier material
selected from silica, alumina, zirconia, titania or mixtures
thereof, other oxides, carbons, carbides and nitrides.
[0016] The process for the production of high-octane gasoline from
a C.sub.6-C.sub.10 hydrocarbon feed can be a combination of a
catalytic dehydrogenation step, a catalytic isomerisation step and
one or more separation steps.
BRIEF DESCRIPTION OF THE DRAWINGS
[0017] FIG. 1 is a schematic flow sheet showing a process for
producing high RON gasoline from a feed containing low amounts of
aromatics.
[0018] FIG. 2 is a schematic flow sheet showing a process for
producing high RON gasoline from a feed containing large amounts of
cyclic compounds.
DETAILED DESCRIPTION OF THE INVENTION
[0019] The main object of the invention is to increase the octane
number of a C.sub.6-C.sub.10 hydrocarbon mixture by dehydrogenation
of cycloparaffins.
[0020] The invention comprises a process, its process conditions
and catalyst suitable for selective conversion of cycloparaffins to
aromatics and hydrogen in presence of paraffins.
[0021] The paraffins must not be affected by the dehydrogenation
reaction. However, they may be converted to high-octane
multi-branched isomers by other processes already known in the art.
Consequently, any reaction of paraffins during the dehydrogenation
step is undesired.
[0022] Multi-branched isomers are defined as compounds containing
more than one carbon atom having more than one side chain on the
main hydrocarbon chain. Mono-branched isomers are defined as
compounds having solely one such side chain.
[0023] Dehydrogenation according to the invention proceeds
selectively without affecting paraffins present in feed when
involving a catalyst comprising a Group VIII metal supported on a
substantially non-acidic porous material with concentration of
acidic sites lower than 1 .mu.mole/g as e.g. determined by known
ammonia TPD desorption.
[0024] The invention is suitable for a process with a
C.sub.6-C.sub.10 hydrocarbon fraction feed consisting mainly of
aromatics, paraffins and cycloparaffins. The feed might originate
from distillation of crude oil, from hydro cracking or from other
refinery units. Thus, various ratios between the components can
occur and the process is designed for operation with both very high
and very low content of cycloparaffins. While aromatics and
paraffins pass the process substantially unchanged, cycloparaffins
are selectively dehydrogenated to aromatics and hydrogen by the
process of the invention.
[0025] Dehydrogenation reaction should proceed under
thermodynamically favourable conditions, i.e. temperatures at least
300.degree. C. As regards the catalyst stability, it might be
beneficial to proceed at temperatures not above 700.degree. C. and
in the presence of hydrogen with a molar hydrogen to hydrocarbon
ratio between 0.1 and 10. Other favourable conditions are a total
pressure varying between 1 and 100 bar and liquid space velocity
LHSV between 0.1 to 1000 h.sup.-1. The preferred conditions are
temperatures between 350-550.degree. C., LHSV between 5-50
h.sup.-1, pressure between 5-50 bar and a molar
hydrogen/hydrocarbon ratio between 1 and 5.
[0026] The catalyst used for dehydrogenation of cycloparaffins in
presence of branched paraffins without their cracking comprises
Group VIII metal on a support, which is not acidic or which has
only very moderate acidity, lower than acidity of for example
silico-alumina. The concentration of strong acidic sites on a
catalyst is defined by ammonia desorption at temperatures higher
than 200.degree. C. This concentration of the catalyst of the
invention must be lower than 1 .mu.mole/g. The support used for
this application can be for example silica, alumina, titania,
zirconia or mixture of these or other oxides as well as various
carbons, carbides, nitrides etc.
[0027] Any metal of group VIII of the periodical system of elements
can be used. However, the most typical materials would be Pt, Pd,
Ir, Rh or a mixture thereof. The loading of the metal can vary
between 0.01% and 5% by weight, preferably between 0.1% and 1% by
weight.
[0028] Dehydrogenation selectivity of the catalyst under the above
specified favourable reaction conditions approaches 100% with
substantially no effect on present paraffins, which pass reactor
non-effected.
[0029] Dehydrogenation of cycloparaffins can be combined in a
multi-stage process with isomerisation without substantial cracking
of produced multi-branched hydrocarbons.
[0030] In such case, the multi-stage process comprises
dehydrogenation of the invention for conversion of cycloalkanes to
hydrogen and aromatics without cracking paraffins, formation of
branched isomers, isomerisation, and separation of multi-branched
isomers and aromatics using e.g. distillation, molecular sieve
membranes, simulated moving bed or pressure swing adsorption.
[0031] In addition to formation of multi-branched paraffins in the
isomerisation process, also conversion of cyclo-pentane derivates
to cyclo-hexane derivates takes place.
[0032] The typical examples of suitable catalysts for isomerisation
of C.sub.6+ paraffins may comprise porous materials based on
tungsten oxide or tungsten containing compounds both supported and
unsupported. The materials are porous having a pore size of 2-50
nm, i.e. mesoporous. The tungsten content is typically between 5%
and 50% by weight. Tungsten oxide catalysts supported on zirconia,
alumina, silica, hafnia, titania or SnO.sub.2 or mixtures of these
are of main interest. However, in principle, all oxides of group VI
elements supported on group IV oxides are potential candidates for
the application. Yet another group of materials applicable are
heteropoly acids consisting of Keggin-ion-structures. The most
typical examples are phosphotungstic and silicotungstic acids.
Friedel-Crafts catalysts based on AlCl.sub.3 can also be used for
this application. Also various zeolites such as zeolite Beta and
Sapo-11 can be used. The catalyst for C.sub.6+ isomerisation must
contain 0.01 wt % to 2 wt % of noble metal. The noble metal would
be most typically Pt or Pd or a mixture thereof. The reaction
proceeds in the presence of hydrogen with a molar hydrogen to
hydrocarbon ratio between 0.1 to 5 at the temperature range from
150.degree. C. to 300.degree. C. with total pressure varying
between 1 and 40 bar and liquid space velocity LHSV between 0.1 to
30 h.sup.-1.
[0033] There are several methods to separate aromatics and
multi-branched isomers from the low octane components like mono and
linear paraffins. For example, U.S. Pat. No. 6,156,950 describes
two-stage unit, which uses zeolite A to separate linear isomers and
MFI zeolite in the next stage to separate multi-branched products
and cyclic compounds. Although the main purpose was to remove
cycloparaffins and aromatics, a product stream was obtained where
linear and mono-branched molecules were only 10% of the paraffins
fraction. U.S. Pat. No. 4,925,459 describes use of zeolite
incorporated in polymer for separation of pentanes. U.S. Pat. No.
6,156,950 shows that linear molecules can also be separated on
zeolite layer supported on ceramics. Yet another process is the use
of chromatography on various zeolite adsorbents. The separation
proceeds by passing the hydrocarbon mixture through the column
filled with molecular sieve and the separated streams of products
are withdrawn in the end of the column. U.S. Pat. Nos. 5,770,783
and 5,744,684 describe a process based on reactive chromatography,
when molecular sieve is mixed with the isomerisation catalyst to
combine separation and reaction step together. Simulated moving bed
is the similar option. Both these methods provide higher
selectivities, but are more difficult to operate than the other
mentioned methods. The choice of the suitable separation technology
is not limited to the above mentioned examples.
DETAILED DESCRIPTION OF THE DRAWINGS
[0034] The total process scheme can be based on the combination of
the two reaction steps described in the above paragraphs and at
least one separation step. All these steps can be combined in
various ways.
[0035] In order to further illustrate the invention, two
embodiments are described below on FIG. 1 and FIG. 2, where R1 is
the dehydrogenation step and R2 is the isomerisation step.
[0036] The first embodiment is shown schematically in FIG. 1. This
process is especially suited for feed containing low amounts of
aromatics. The hydrocarbon feedstock is passed via line 1 to the
isomerisation unit R2. In R2 linear paraffins and mono-branched
paraffins are isomerised to multi-branched paraffins simultaneously
with cyclo-pentane derivates being converted to cyclo-hexane
paraffins. The effluent from R2 comprising multi-branched isomers
and cycloparaffins is passed in line 2 to the dehydrogenation unit
R1.
[0037] In R1 the dehydrogenation process of the invention will
convert cyclo-alkanes to aromatic compounds without any conversion
of the multi-branched paraffins. Since cyclo-hexane derivates are
far more reactive in the dehydrogenation reaction than
cyclo-pentane derivates, the isomerisation of cyclo-pentane
derivates to cyclo-pentane derivates in the isomerisation step
favours conversion to aromatics in the dehydrogenation step.
[0038] The effluent from R1 is passed via line 3 to a flash
section, from where gases leave the process in line 4. The fluid
gasoline phase is passed from the flash section via line 5 to
separation step S, where the high octane number product, comprising
aromatics and multi-branched paraffins, is separated from a recycle
stream. The product leaves the process via line 6 and the recycle
stream consisting predominantly of non-converted cyclo-alkanes,
linear and mono-branched paraffins, is via line 7 led to R2.
[0039] The dehydrogenation of the invention used in this process
makes it possible first to create multi-branched paraffins from the
feed and from the recycle and then to improve the gasoline by
converting cyclo-alkanes to aromatics without cracking the
multi-branched paraffins.
[0040] By this, only non-converted cyclo-alkanes, linear and
mono-branched paraffins are recycled. The product can contain 90%
of the multi-branched paraffins and only 10% of the mono-branched
paraffins, the rest is recycled to the isomerisation.
[0041] Another embodiment is shown on FIG. 2. This process is
particularly useful for feed containing large amounts of cyclic
compounds. In this case the hydrocarbon feedstock is passed via
line 1 to the dehydrogenation unit R1, where the cyclic compounds
are converted to aromatic compounds. The effluent from R1
comprising predominantly linear, mono-branched and multi-branched
isomers and aromatics is passed via line 2 to a flash unit. Here
gas and hydrogen flash off, while the liquid phase gasoline flows
via line 3 to a separation unit, S. In S, the product is separated
from the remainder part of the gasoline.
[0042] From S, the product comprising aromates, multi-branched
paraffins and a small amount of cyclo-branched and mono-branched
paraffins is withdrawn in line 4. The separation is carried out so
90% of the multi-branched paraffins and only 10% of the
mono-branched paraffins leave the process in the product stream 4.
The remainder, comprising mainly non-converted cyclic compounds,
linear and mono-branched paraffins, is passed via line 5 to the
isomerisation unit, R2, where these paraffins are converted to
multi-branched paraffins.
[0043] As mentioned above, in the flash unit hydrogen and gas are
separated from the gasoline. This gas and hydrogen is passed in
line 6 to a separation, where the gas is withdrawn from the process
via line 7. The hydrogen stream is split-up in a stream
corresponding to the produced amount of surplus, which is withdrawn
in line 8 and in a stream, which supplies the isomerisation unit R2
with the required amount of hydrogen.
[0044] In R2 the linear and mono-branched paraffins are converted
to multi-branched paraffins and cyclo-pentane derivates to
cyclo-hexane derivates, and the effluent is passed via line 9 to
the dehydrogenation R1. The dehydrogenation of the invention will
then create aromatic compounds without converting the produced
multi-branched paraffins.
[0045] The advantage of using the dehydrogenation of the invention
in this process, shown on FIG. 2, is that the invention makes it
possible to convert the cyclo-alkanes to aromatic compounds without
destroying the valuable multi-branched paraffins. And thereafter to
separate the high octane number product from the recycle stream
which then can be isomerised.
[0046] Thereby, isomerisation takes place without any aromatic
compounds being present and thereby hydrogenation of these aromatic
compounds to cyclic compounds is avoided.
[0047] As apparent from the above description, the invention makes
it possible to produce high-octane gasoline in a process with few
steps.
EXAMPLE 1
[0048] 10 g of commercial alumina MAG-42 (Sasol Ltd) are
impregnated with 0.7% Pt, 0.3% Pd and calcined at 350.degree. C.
Afterwards, the catalyst was exchanged with 1 N Na.sub.2CO.sub.3
solution.
[0049] The feed used in the reaction is a C.sub.7 cut consisting of
36 wt % methylcyclohexane and 64% of heptanes. The detail
composition is shown in Table 1. The reaction is performed in a
fixed bed reactor at 400.degree. C. with LHSV=1 h.sup.-1 at the
total pressure of 7 bar and the feed consisting of a
hydrocarbon:hydrogen mixture with the molar ratio of 1:4. The
detailed feed and product compositions are shown in Table 1.
[0050] The example shows that cycloparaffins can be selectively
converted to aromatics in presence of branched paraffins without
cracking them to gas. Such reaction results in significantly higher
octane number of the product.
1TABLE 1 Feed and product compositions referring to dehydrogenation
of Example 1 Feed [wt %] Product [wt %] Methane -- 0.07 Propane --
0.15 Isobutane -- 0.17 Hexanes -- 0.26 Benzene -- 0.15 Cyclohexane
-- 0.03 2,4-dimethylpentane 43.9 41.0 3,3-dimethylpentane 0.2 0.3
2-methylhexane 0.3 0.3 2,3-dimethylpentane 17.8 18.3 3-methylhexane
-- 0.3 3-ethylpentane -- -- n-heptane -- 0.1 Methylcyclohexane 36.0
3.8 Toluene -- 35.1 RON - calculated 79.9 91.1
EXAMPLE 2
[0051] 10 g of commercial alumina MAG-42 are impregnated with 0.05%
Pt and 0.05% Rh and calcined at 350.degree. C. Afterwards, the
catalyst was treated with 1% wt of KCl and excess of water
evaporated.
[0052] The feed used in the reaction is a C.sub.7 cut consisting of
37 wt % methyl-cyclohexane and 63% of n-heptane. The detailed
composition is shown in Table 2. The reaction is performed in a
fixed bed reactor at 400.degree. C. with LHSV=120 h.sup.-1 at the
total pressure of 10 bar and the feed consisting of a
hydrocarbon:hydrogen mixture with the ratio of 1:2. The detailed
feed and product compositions are shown in Table 2.
[0053] The example shows that cycloparaffins can be selectively
converted to aromatics in presence of linear paraffins without
cracking them to gas. Such reaction results in significantly higher
octane number of the product.
2TABLE 2 Feed and product compositions referring to dehydrogenation
of Example 2 Feed [wt %] Product [wt %] Methane -- 0.05 Propane --
0.03 Butanes -- 0.15 Hexanes 0.1 0.15 Benzene -- -- Cyclohexane --
-- 2,4-dimethylpentane -- -- 3,3-dimethylpentane -- --
2-methylhexane -- 0.1 2,3-dimethylpentane -- -- 3-methylhexane --
0.2 3-ethylpentane -- -- n-heptane 62.8 62.1 Methyl-cyclohexane
37.1 1.6 Toluene -- 35.6 RON - calculated 27.9 42.5
EXAMPLE 3
[0054] Zirconium oxide was prepared by adding diluted ammonia to a
water solution of zirconyl nitrate and adjusting pH to 9. The
mixture was refluxed overnight. The white solid was filtered and
washed and dried overnight at 120.degree. C. The dried material had
surface area of 333 m.sup.2/g. 225 g of zirconia, 168 g alumina gel
(pseudoboehmite 30 wt %) and 62 g of ammonium metatungstate were
milled for 15 minutes and {fraction (1/16)}" extrudates were
prepared under 12 bar pressure. The catalyst was calcined at
700.degree. C. for three hours and 0.5 wt % Pd was introduced by
incipient wetness impregnation. The catalyst was calcined at
350.degree. C. before it was placed into the reactor.
[0055] Heptane isomerisation with the above described catalyst was
performed in a fixed bed reactor at 165.degree. C. with LHSV=0.2
h.sup.-1 at a total pressure of 7 bar and the feed consisting of a
hydrogen:hydrocarbon mixture with the ratio of 1:2. A detailed
description of the product composition is shown in Table 3.
[0056] The catalyst produced on a once-through basis 35.1% of
multi-branched isomers with only 3.2% cracking (liquid yield 92%).
Calculated RON of the multi-branched isomer fraction is 89.2.
3TABLE 3 n-Heptane isomerisation at 165.degree. C. with LHSV = 0.2
h.sup.-1 at a total pressure of 7 bar and the feed consisting of a
hydrogen:hydrocarbon mixture of a ratio of 1:2 Product [wt %]
Propane 1.34 Isobutane 1.74 n-Butane 0.07 Isopentane 0.03
Isohexanes 0.03 2,2-dimethylpentane 11.66 2,4-dimethylpentane 9.02
2,2,3-trimethylbutane 1.22 3,3-dimethylpentane 4.84 2-methylhexane
25.52 2,3-dimethylpentane 8.32 3-methylhexane 23.2 3-ethylpentane
1.49 n-heptane 11.30 Cycloheptanes 0.10
* * * * *