U.S. patent number 3,843,741 [Application Number 05/384,317] was granted by the patent office on 1974-10-22 for aromatization process and catalyst therefor.
This patent grant is currently assigned to Mobil Oil Corporation. Invention is credited to Tsoung-Yuan Yan.
United States Patent |
3,843,741 |
Yan |
October 22, 1974 |
**Please see images for:
( Certificate of Correction ) ** |
AROMATIZATION PROCESS AND CATALYST THEREFOR
Abstract
Improvements in the aromatization of hydrocarbon streams by
contact thereof with a ZSM-5 type of synthetic aluminosilicate
zeolite catalyst at elevated temperatures of about 500.degree. to
1500.degree.F, in the absence of added hydrogen, at high severities
to convert at least 80 weight percent of the feed to a product, the
liquid portion of which comprises aromatics, which improvement is
engendered by utilizing a matrix catalyst containing said zeolite
in a high silica content binder.
Inventors: |
Yan; Tsoung-Yuan (Trenton,
NJ) |
Assignee: |
Mobil Oil Corporation (New
York, NY)
|
Family
ID: |
23516845 |
Appl.
No.: |
05/384,317 |
Filed: |
July 31, 1973 |
Current U.S.
Class: |
585/407; 208/138;
208/135; 585/418 |
Current CPC
Class: |
B01J
29/46 (20130101); B01J 29/40 (20130101); C10G
35/095 (20130101); B01J 29/405 (20130101); B01J
2229/36 (20130101); B01J 2229/26 (20130101); B01J
2229/42 (20130101) |
Current International
Class: |
C10G
35/00 (20060101); C10G 35/095 (20060101); B01J
29/40 (20060101); B01J 29/00 (20060101); B01J
29/46 (20060101); C07c 003/02 () |
Field of
Search: |
;260/673,673.5
;308/137,135 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Gantz; Delbert E.
Assistant Examiner: Nelson; Juanita M.
Attorney, Agent or Firm: Gaboriault; Andrew L. Gilman;
Michael G.
Claims
What is claimed is:
1. In the process of converting an aliphatic feedstock having an
atmospheric boiling point of up to about 400.degree.F to aromatic
hydrocarbons by contacting such feedstock with a ZSM-5 type of
zeolite at about 500.degree. to 1500.degree.F and a space velocity
of up to about 15 WHSV; the improvement, whereby inhibiting the
formation of coke on said catalyst and improving the steam
stability of the said catalyst, comprising using as said catalyst a
matrix of ZSM-5 type of crystalline zeolite and a second, inorganic
component consisting essentially of at least about 80 weight
percent silica.
2. The improved process claimed in claim 1 wherein said zeolite is
ZSM-5.
3. The improved process claimed in claim 1 wherein said second
component is silica.
4. The improved process claimed in claim 1 wherein said feedstock
comprises olefinic hydrocarbons and said aromatization temperature
is at least about 650.degree.F.
5. The improved process claimed in claim 1 wherein said feedstock
comprises paraffinic hydrocarbons and said aromatization
temperature is at least about 850.degree.F.
6. The improved process claimed in claim 1 wherein said matrix
comprises about 1 to 95 weight percent zeolite.
7. The improved process claimed in claim 1 wherein said zeolite is
Zn ZSM-5.
8. The improved process claimed in claim 1 wherein said zeolite is
Zn Cu ZSM-5.
9. The improved process claimed in claim 1 including depositing
coke on said catalyst at a rate of up to about 1 gram per 100 grams
of carbon in the feed.
10. The improved process claimed in claim 1 wherein said catalyst
has a zeolite to matrix material ratio of about 0.01 to 20 to 1.
Description
This invention relates to hydrocarbon conversion. It more
particularly refers to improvements in the art of converting
aliphatic petroleum and/or other chemical fractions to
aromatics.
There has recently been developed a commercially feasible process
for upgrading aliphatic petroleum feedstocks. According this
process a C.sub.2 to 400.degree.F feed, or any given portion
thereof is contacted with a ZSM-5 type of synthetic aluminosilicate
zeolite at about 650.degree. to 1500.degree.F (depending upon the
specific composition of the feed) at a space velocity of up to
about 15 WHSV, and in the substantial absence of added hydrogen,
under such combination of conditions as to convert substantial
portions of the nonaromatic portions of the feed to a mixed gas and
liquid product, which liquid product contains new aromatics in a
proportion of at least about 30 grams per 100 grams of the
non-aromatic portion of the feed. Reference is made to applications
Ser. Nos. 153,885 now U.S. Pat. No. 2,756,942 and 253,942 now U.S.
Pat. No. 3,756,942 filed June 16, 1971 and May 17, 1972
respectively. The full text of these commonly assigned prior
applications is incorporated herein by reference.
Feedstocks for use in this process are illustrated by Udex
raffinates, coker gasoline, light cracked gasoline, straight run
naphthas, pyrolysis gasoline and the like. These feeds are usually
aliphatic in nature being composed of paraffins, olefins and
naphthenes. Aromatics may be present in the feedstock to any extent
considered to be desirable. Since they are often substantially
inert under these processing conditions their proportion may be
limited. An oxygen containing gas can be admixed with the feed,
such as air, oxygen, oxygen diluted by an inert gas or gases or air
enriched with the oxygen. The feed may be or contain oxygenated
moieties such as partially oxidized light gases, or even be
oxygenated organic chemical compounds such as acetone,
acetaldehyde, methanol or the like. It is also within the scope of
this invention to utilize organic compound feeds having a lower
aliphatic portion and a hetero portion, such as sulfur, halogen or
nitrogen.
The catalyst used for this known process has been stated to be a
ZSM-5 type of catalyst which includes ZSM-5, ZSM-8, ZSM-11 and
other similarly behaving zeolites.
ZSM-5 is disclosed and claimed in copending application Ser. No.
865,462, now U.S. Pat. No. 3,702,886 filed Oct. 10, 1969; ZSM-8 is
disclosed and claimed in copending application Ser. No. 865,418,
filed Oct. 10, 1969 and ZSM-11 is disclosed and claimed in
copending application Ser. No. 31,421 filed Apr. 23, 1970.
The family of ZSM-5 compositions has the characteristic x-ray
diffraction pattern set forth in Table 1 hereinbelow. ZSM-5
compositions can also be identified, in terms of mole ratios of
oxides, as follows:
0.9 .+-. 0.2 M.sub.2/n O: W.sub.2 O.sub.3 : b YO.sub.2 : z H.sub.2
O
wherein M is a cation, n is the valence of said cation, W is
selected from the group consisting of aluminum and gallium, Y is
selected from the group consisting of silicon and germanium, z is
from 0 to 40 and b is at least 5 and preferably 15-300. In a
preferred synthesized form, the zeolite has a formula, in terms of
mole ratios of oxides, as follows:
0.9 .+-. 0.2 M.sub.2/n 0 : Al.sub.2 O.sub.3 : 5-100 SiO.sub.2 : z
H.sub.2 O
and M is selected from the group consisting of a mixture of alkali
metal cations, especially sodium and tetraalkylammonium cations,
the alkyl groups of which preferably contain two to five carbon
atoms.
In a preferred embodiment of ZSM-5, W is aluminum, Y is silicon and
the silica/alumina mole ratio is at least 15, preferably at least
30.
Members of the family of ZSM-5 zeolites which include ZSM-5, ZSM-8
and ZSM-11 possess a definite distinguishing crystalline structure
whose x-ray diffraction pattern shows the following significant
lines:
Table 1 ______________________________________ Interplanar Spacing
d(A) Relative Intensity ______________________________________ 11.1
.+-. 0.3 S 10.0 .+-. 0.25 S 7.4 .+-. 0.2 W 7.1 .+-. 0.15 W 6.3 .+-.
0.1 W 6.04 .+-. 0.1 W 5.97 .+-. 0.1 W 5.56 .+-. 0.1 W 5.01 .+-. 0.1
W 4.60 .+-. 0.08 W 4.25 .+-. 0.08 W 3.85 .+-. 0.07 VS 3.71 .+-.
0.05 S 3.64 .+-. 0.05 M 3.04 .+-. 0.04 W 2.99 .+-. 0.03 W 2.94 .+-.
0.02 W ______________________________________
These values, as well as all other x-ray data were determined by
standard techniques. The radiation was the K-alpha doublet of
copper, and a scintillation counter spectrometer with a strip chart
pen recorder was used. The peak heights, I, and the positions as a
function of 2 times theta, where theta is the Bragg angle, were
read from the spectrometer chart. From these the relative
intensities, 100 I/I.sub.o, where I.sub.o is the intensity of the
strongest line or peak, and d(obs.), the interplanar spacing in A,
corresponding to the recorded lines, were calculated. In Table 1
the relative intensities are given in terms of the symbols S =
strong, M = medium, MS = medium strong, MW = medium weak and VS =
very strong. It should be understood that this x-ray diffraction
pattern is characteristic of all the species of ZSM-5 compositions.
Ion exchange of the sodium ion with cations reveals substantially
the same pattern with some minor shifts in interplanar spacing and
variation in relative intensity. Other minor variations can occur,
depending on the silicon to aluminum ratio of the particular
sample, as well as if it has been subjected to thermal
treatment.
Zeolite ZSM-5 can be suitably prepared by preparing a solution
containing water, tetrapropyl ammonium hydroxide and the elements
of sodium oxide, an oxide of aluminum or gallium and an oxide of
silica, and having a composition, in terms of mole ratios of
oxides, falling within the following ranges:
TABLE 2 ______________________________________ Particularly Broad
Preferred Preferred ______________________________________
OH.sup.-/SiO.sub.2 0.07-1.0 0.1-0.8 0.2-0.75 R.sub.4 N+/(R.sub.4
N.sup.++Na.sup.+) 0.2-0.95 0.3-0.9 0.4-0.9 H.sub.2 O/OH.sup.-
10-300 10-300 10-300 YO.sub.2 /w.sub.2 O.sub.3 5-100 10-60 10-40
______________________________________
Wherein R is propyl, W is aluminum and Y IS silicon. This mixture
is maintained at reaction conditions until the crystals of the
zeolite are formed. Thereafter the crystals are separated from the
liquid and recovered. Typical reaction conditions consist of a
temperature of from about 75.degree.C to 175.degree.C for a period
of about six hours to 60 days. A more preferred temperature range
is from about 90.degree. to 150.degree.C, with the amount of time
at a temperature in such range being from about 12 hours to 20
days.
The digestion of the gel particles is carried out until crystals
form. The solid product is separated from the reaction medium, as
by cooling the whole to room temperature, filtering and water
washing.
ZSM-5 is preferably formed as an aluminosilicate. The composition
can be prepared utilizing materials which supply the elements of
the appropriate oxide. Such compositions include, for an
aluminosilicate, sodium aluminate, alumina, sodium silicate, silica
hydrosol, silica gel, silicic acid, sodium hydroxide and
tetrapropylammonium hydroxide. It will be understood that each
oxide component utilized in the reaction mixture for preparing a
member of the ZSM-5 family can be supplied by one or more initial
reactants and they can be mixed together in any order. For example,
sodium oxide can be supplied by an aqueous solution of sodium
hydroxide, or by an aqueous solution of sodium silicate;
tetrapropylammonium cation can be supplied by the bromide salt. The
reaction mixture can be prepared either batchwise or continuously.
Crystal size and crystallization time of the ZSM-5 composition will
vary with the nature of the reaction mixture employed.
ZSM-8 can also be identified, in terms of mole ratios of oxides, as
follows:
0.9 .+-. 0.2 M.sub.2/n O : Al.sub.2 O.sub.3 : 5-300 SiO.sub.2 : z
H.sub.2 O
wherein M is at least one cation, n is the valence thereof and z is
from 0 to 40. In a preferred synthesized form, the zeolite has a
formula, in terms of mole ratios of oxides, as follows:
0.9 .+-. 0.2 M.sub.2/n O : Al.sub.2 O.sub.3 : 15-60 SiO.sub.2 : z
H.sub.2 O
and M is selected from the group consisting of a mixture of alkali
metal cations, especially sodium, and tetraethylammonium
cations.
Zeolite ZSM-8 can be suitably prepared by reacting a water solution
containing either tetraethylammonium hydroxide or
tetraethylammonium bromide together with the elements of sodium
oxide, aluminum oxide, and an oxide of silica.
The operable relative proportions of the various ingredients have
not been fully determined and it is to be immediately understood
that not any and all proportions of reactants will operate to
produce the desired zeolite. In fact, completely different zeolites
can be prepared utilizing the same starting materials depending
upon their relative concentration and reaction conditions as is set
forth in U.S. Pat. No. 3,308,069. In general, however it has been
found that when tetraethylammonium hydroxide is employed, ZSM-8 can
be prepared from said hydroxide, sodium oxide, aluminum oxide,
silica and water by reacting said materials in such proportions
that the forming solution has a composition in terms of mole ratios
of oxides falling within the following ranges:
SiO.sub.2 /Al.sub.2 O.sub.3 -- from about 10 to about 200
Na.sub.2 O/tetraethylammonium hydroxide -- from about 0.05 to
.020
Tetraethylammonium hydroxide /SiO.sub.2 -- from about 0.08 to
1.0
H.sub.2 o/tetraethylammonium hydroxide -- from about 80 to about
200
Thereafter, the crystals are separated from the liquid and
recovered. Typical reaction conditions consist of maintaining the
foregoing reaction mixture at a temperature of from about
100.degree.C to 175.degree.C for a period of time of from about six
hours to 60 days. A more preferred temperature range is from about
150.degree. to 175.degree.C with the amount of time at a
temperature in such range being from about 12 hours to 8 days.
ZSM-11 can also be identified, in terms of mole ratios of oxides,
as follows:
0.9 .+-. 0.3 M.sub.2/n O : Al.sub.2 O.sub.3 : 20-90 SiO.sub.2 : z
H.sub.2 O
wherein M is at least one cation, n is the valence thereof and z is
from 6 to 12. In a preferred synthesized form, the zeolite has a
formula, in terms of mole ratios of oxides, as follows:
0.9 .+-. 0.3 M.sub.2/n O : Al.sub.2 O.sub.3 : 20-90 SiO.sub.2 : z
H.sub.2 O
and M is selected from the group consisting of a mixture of alkali
metal cations, especially sodium, and tetrabutylammonium
cations.
ZSM-11 can be suitably prepared by preparing a solution containing
(R.sub.4 X).sub.2 O, sodium oxide, an oxide of aluminum or gallium,
an oxide of silicon or germanium and water and having a
composition, in terms of mole ratios of oxides, falling within the
following ranges:
Broad Preferred ______________________________________ YO.sub.2
/WO.sub.2 10-150 20-90 Na.sub.2 O/YO.sub.2 .05-0.7 0.05-0-40
(R.sub.4 X).sub.2 O/YO.sub.2 0.02- 0.20 0.02-0.15 H.sub.2
O/Na.sub.2 O 50-800 100-600
______________________________________
wherein R.sub.4 X is a cation of a quaternary compound of an
element of Group 5A of the Periodic Table, W is aluminum or gallium
and Y is silicon or germanium maintaining the mixture until
crystals of the zerolite are formed. Preferably, crystallization is
performed under pressure in an autoclave or static bomb reactor.
The temperature ranges from 100.degree.C-200.degree.C generally,
but at lower temperatures, e.g. about 100.degree.C crystallization
time is longer. Thereafter the crystals are separated from the
liquid and recovered. The new zeolite is preferably formed in an
aluminosilicate form.
An embodiment of this catalyst resides in the use of a porous
matrix together with the ZSM-5 type family of zeolite previously
described. The zeolite can be combined, dispersed, or otherwise
intimately admixed with the porous matrix in such proportions that
resulting products contain from 1 to 95 percent by weight and
preferably from 10 to 70 percent by weight of the zeolite in the
final composite.
The term "porous matrix" includes non-zeolite inorganic
compositions with which the zeolites can be combined, dispersed or
otherwise intimately admixed wherein the matrix may be
catalytically active or inactive. It is to be understood that the
porosity of the composition employed as a matrix can be either
inherent in the particular material or it can be introduced by
mechanical or chemical means. Representative of matrices which can
be employed include metals and alloys thereof, sintered metals, and
sintered glass, asbestos, silicon carbide, aggregates, pumice,
firebrick, diatomaceous earths, alumina, and inorganic oxides.
Inorganic compositions, especially those comprising alumina and
those of a siliceous nature are preferred. Of these matrices
inorganic oxides such as clay, chemically treated clays, silica,
silica alumina, etc. as well as alumina, are particularly preferred
because of their superior porosity, attrition resistance and
stability.
Techniques for incorporating the ZSM-5 type family of zeolites into
a matrix are conventional in the art and are set forth in U.S. No.
3,140,253.
It is to be noted that when a ZSM-5 type zeolite is used in
combination with a porous matrix, space velocities which may be set
forth as parameters for this process are based on the ZSM-5 type
zeolite alone and the porous matrix is ignored. Thus, whether a
ZSM-5 type zeolite is used alone or in a porous matrix, the space
velocities in all cases refer to the ZSM-5 type component.
It is known that zeolites, particularly synthetic zeolites can have
their composition modified by impregnating certain metals thereonto
and/or thereinto. The composition can also be modified by
exchanging various anions and/or cations into the crystal structure
of the zeolite, replacing more or less of the ions originally
present upon production of the zeolite.
The ZSM-5 type family of zeolites have been found to be especially
active for aromatization if they have at least a portion of the
original cations associated therewith replaced by any of a wide
variety of other cations according to techniques well known in the
art. Typical replacing cations would include hydrogen, ammonium,
and metal cations, including mixtures of the same. Of the replacing
cations, preference is given to cations of hydrogen, ammonium, rare
earth, magnesium, zinc, calcium, nickel, copper and mixtures
thereof. Particularly effective members of the ZSM-5 type family of
zeolites are those which have been base exchanged with hydrogen
ions, ammonium ions, zinc ions or mixtures thereof. Most especially
zinc ZSM-5 is the best presently known catalyst for aromatizations
as set forth.
Typical ion exchange techniques would be to contact a ZSM-5 type of
zeolite with a salt of the desired replacing cation or cations.
Although a wide variety of salts can be employed, particular
preference is given to chlorides, nitrates and sulfates.
Representative ion exchange techniques are disclosed in a wide
variety of patents, including U.S. Pat. Nos. 3,140,249; 3,140,251;
and 3,140,253.
It is also within the scope of the aromatization process to which
this application is directed to incorporate a desired metallic
component onto the ZSM-5 type family of zeolites by techniques
other than ion exchange. Thus, for example, it is possible to
impregnate a desired metallic component, such as zinc, platinum or
palladium, thereinto by conventional impregnation techniques, as
well as merely depositing the elemental metal onto the particular
zeolite and in some cases, such as with zinc oxide, to incorporate
the metal by physical admixture of the zeolite with an insoluble
metal compound.
In any event, following contact with a salt solution of the desired
replacing cation, the zeolites are preferably washed with water and
dried at a temperature ranging from 150.degree. to about
600.degree.F and thereafter heated in air or inert gas at
temperatures ranging from about 500.degree.F to 1500.degree.F for
periods of time ranging from 1 to 48 hours or more. It is noted
that this heat treatment can be carried out in situ, i.e. while the
particular aromatization reaction is taking place, but it is
preferred to carry it out as a separate step prior to carrying out
the aromatization reaction.
One of the problems presently being coped with in carrying out the
process described above stems from the fact that during the
hydrocarbon conversion, the solid catalyst has a certain proportion
of coke deposited thereon. As the proportion of deposited coke
increases, the activity of the catalyst decreases until a point is
reached at which it becomes expedient to regenerate the catalyst.
This regeneration usually involves burning off the deposited coke
with air. The steam generated in this oxidative regeneration step
may irreversibly damage the catalyst activity and sometimes results
in short ultimate catalyst life. It is obvious that the economics
of such a cyclic process will be improved in direct proportion to
the length of time the catalyst can be kept on stream between
regenerations and ultimate life of the catalyst (i.e. number of
regeneration cycles possible).
It is therefore an object of this invention to provide a novel
aromatization process utilizing an improved catalyst
composition.
Other and additional objects of this invention will become apparent
from a consideration of this entire specification including the
claims hereof.
In accord with and fulfilling these objects, one aspect of this
invention resides in carrying out an aromatization conversion of
aliphatic organic compounds in the effective presence of am
improved catalyst comprising a matrix of a ZSM-5 type of synthetic
aluminosilicate zeolite and a second inorganic material consisting
essentially of at least about 80 percent silica.
It is known to provide ZSM-5 type of zeolites as a porous matrix by
intimately mixing about 1 to 95 weight percent of the zeolite with
an appropriate porous matrix material preferably about 10 to 70
percent ZSM-5. Application Ser. No. 253,942 now U.S. Pat. No.
3,756,942 set forth above reveals representative matrix materials
as metals, alloys, sintered metals, sintered glass, asbestos,
silicon carbide, aggregates, pumice, firebrick, diatomaceous
earths, aluminasilica and/or other inorganic oxides. This prior
application indicates that inorganic oxides., especially alumina,
clay, silica-alumina and silica are considered to be preferred
because of their superior porosity attrition resistance and
stability. It was belived that the exact chemical nature of the
matrix material was not particularly important but that the
porosity was the controlling factor in evaluating suitable matrix
materials for admixture with ZSM-5 zeolites. While it was
originally thought that silica, alumina and silica-alumina or
various proportions were of similar behavior in relation to ZSM-5
catalysts, it has now been discovered that this is not so and that
there is indeed a dramatic difference in the coking tendency and
steaming stability of these various matrix materials.
Therefore, it is one aspect of this invention to carry out an
aromatization conversion utilizing a high silica bonded ZSM-5 type
of zeolite catalyst. While silica, silica-alumina and alumina are
all relatively inert materials with respect to the feed materials
disclosed herein at ordinary temperatures, at aromatization
temperatures, alumina and silica-alumina have been found to
catalyze conversion of these feeds into coke in relatively large
proportions. On the other hand, silica appears to continue to be
substantially inert not only at ordinary temperatures but at
aromatization temperatures as well.
According to this invention, an aromatizable feedstock having a
boiling point at atmospheric pressure of up to about 400.degree.F,
which may be hydrocarbon or one or more hetero atom containing
organic compounds (e.g., an aliphatic organic compound having an
oxygen, nitrogen, halogen or sulfur hetero atom or atoms
constituent therein), and which may or may not be admixed with
hydrogen or an oxygen containing gas, is converted to a highly
aromatic product by effective contact thereof with a matrix
cataylst comprising a ZSM-5 type of zeolite and a second, inorganic
member consisting essentially of at least about 80 percent silica,
and having a zeolite to second member ratio of about 0.01 to 20 to
1, at about 500.degree. to 1500.degree.F, depending upon feedstock
composition and a space velocity of up to about 15 WHSV, under such
combination of conditions as to convert at least about 80 percent
of the feed material to a product which is at least about 35 weight
percent liquid and the remainder gas, while the liquid portion of
such product consists of at least about 80 weight percent of new
aromatics. These new aromatics should represent a yield of at least
about 20 grams per 100 grams of aromatizable feed.
A most important aspect of this invention is the fact that less
coke is formed on the catalyst when operating the hereindefined
process. Therefore a most important operating parameter and a
critical measure of the value of this conversion is that the coke
deposit on the catalyst be at a rate not to exceed 1 gram per 100
grams of carbon in the feed and 100 grams of coke per 100 grams of
the catalyst. For purposes of this coke deposition parameter, feed
should be considered only for its carbon content. A preferred
deposition rate is less than about 0.6 grams per 100 grams of
carbon feed and 60 grams of coke per 100 grams of the catalyst.
According to the process of this invention, the catalyst can be
kept on stream for at least about 50 to 100 grams of feed (that is
for the product of the feed rate and the total on stream time) per
gram of catalyst. The conversion reaction may be carried out with
an upflow or downflow reactor. The catalyst bed may be fixed,
fluidized or moving as desired. The catalyst matrix particle size
will be determined by the type of bed chosen. Generally, catalyst
particle sizes will range from about 4 to about 400 mesh,
preferably about 60 to 400 mesh for fluid bed operation, and about
4 to about 24 mesh for fixed bed operation.
The high silica matrix catalyst of this invention is made by
conventional zeolite catalyst matrix production techniques. In this
regard reference is made to the general discussion on ZSM-5 type of
catalyst, infra. The catalyst is regenerated by contact with an
oxidizing atmosphere at elevated temperatures. Conventional
regeneration with steam and/or air is considered to be
acceptable.
Since this particular hydrocarbon conversion reaction may be
endothermic, exothermic or heat balanced depending upon feed
composition, provision should be made for heat transfer within the
system. This can be accomplished by indirect heat exchange with a
suitable fluid. Heating, if needed, can be accomplished by direct
firing as in a furnace. It can also be accomplished by direct heat
exchange by means of the heated, regenerated catalyst and/or a
preheating of the feed, and/or heating or cooling a recycle
stream.
This invention will be illustrated by the following Examples which
are in no way to be considered to be limiting on the scope thereof.
Parts and percentages are by weight unless expressly stated to be
on some other basis.
EXAMPLES 1 - 4
In each of these Examples ZSM-5 catalyst was prepared and matrixed
with a particular proportion of a specific binder as set forth in
the following Table. Each catalyst matrix was loaded into a fixed
bed reactor through which pyrolysis gasoline was passed at
atmospheric pressure and 1000.degree.F for 2 hours.
TABLE 1
__________________________________________________________________________
Example No. 1 2 3 4 Wt. % H ZSM-5 65 10 65 10 Binder Alumina
Silica/Alumina Silica Silica WHSV 12 10.6 8.3 8.3 Coke Wt. % of
16.9 13.7 6.75 2.0 Catalyst
__________________________________________________________________________
These Examples illustrate the fact that even under increasingly
severe conditions, the replacement of alumina with silica in the
catalyst matrix of this invention reduces the coke make on the
catalyst hereof.
EXAMPLES 5 and 6
Zinc and copper promoted ZSM-5 matrixes with silica and alumina
binders respectively were used to convert C.sub.6 to 200.degree.F.
light virgin naphtha to aromatics. The above defined mid-continent
light naphtha was passed through the catalyst bed at 1000.degree.F,
1 LHSV, atmospheric pressure and no added hydrogen for 18 hours
after which the naphtha feed was stopped and the catalyst was
regenerated with air and then steam at 1000.degree.F and 35 mm Hg
water pressure. After each various length of steaming time, the
catalyst activity was tested. The ability of the catalyst to
convert naphtha to aromatics, reported as aromatics yield, is a
measure of the quality of the catalysts. The curves of FIG. 1 show
the improvement obtained by using a silica binder as opposed to an
alumina binder.
These same tests have been analyzed and the data reported below in
Table 2 on the basis of loss of aromatic yield as a function of
steaming time:
Table 2 ______________________________________ Aromatics Yield Loss
(% of Fresh Activity vs. Steaming
______________________________________ Time) Steaming Time, Hrs.
100 200 300 400 Silica Binder 3.4 6.7 8 8.9 Alumina Binder 7.1 13.6
16.8 19.5 ______________________________________
* * * * *