Note: Descriptions are shown in the official language in which they were submitted.
PROCESS OR T~E PREPARATION OF HYDROCARBO~S
The invention relates to a process for the preparation
of a hydrocarbon mixture boiling in the gasoline range
from a mixture of carbon monoxide and hydrogen.
Hydrocarbcn mixtures boiling in the gasoline range
may, inter alia, be obtained by straight-run distillation
of crude mineral oil, by conversion of heavier crude
mineral oil fractions, for ;nstance by catalytic cracking,
thermal cracking and hydrocracking. and by conversion
of lighter mineral oil fractions, for instance by alkylation.
To improve the octane number of the hydrocarbon mixtures
thus obtained, they are often subjected to catalytic
reforming, which increases the aromatics content.
In view of the decreasing mineral oil reserves, there
is a great interest in pro~esses for the conversion, in
an economically justified way, of carbon-containing materia]s
not based on mineral oi], such as coal, into hydrocarbon
mixtures boiling in the gasoline range. It i.s desirable
that the said hydrocarbon mixtures have a suff;ciently
high octane number so that they can be used as gasoline
without any further refininK.
It is known that carbon-containing materials such as
coal can be converted into mixtures of carbon monoxide
and hydrogen by gasification. It is a]so known that mixtures
of ~arbon monox de and hydrogen c_n be converted into
mixtures of hydrocarbons by contacting the gas mixtures
l~Z~76~7~
with suitable catalysts. It is further known that paraffinic
hvdrocarbons can be converted by partial dehydrogenation or
partial oxidation into olefinic hydrocarbon mixtures and
oxygen-containing hydrocarbon mixtures, respectively.
Finally, it is known that aromatic hydrocarbon mixtures
boiling in the gasoline range can be prepared by contacting
olefinic hydrocarbon mixtures and oxygen-containing hydro-
carbon mixtures with suitable catalysts.
The Applicant has carried out an investigation to
find out to what extent the above-mentioned processes
can be used in the preparation of gasoline from a mixture
of carbon monoxide and hydrogen. It was found in this
investigation that gasoline with a high octane number can
be prepared in a high yield from a mixture of carbon
monoxide and hydrogen by a combination of the above-men-
tioned processes, provided that the following conditions
are satisfied.
First o~ all, an aromatic hydrocarbon mixture should
be prepared ~rom the mixture of carbon monoxide and
2~ hydrogen by using a catalyst which contains a crystalline
silicate, which silicate is characterized in that it has
the following properties after 1 hour's calcining in air at
500C:
7~
(1) thermally s~able at a temperature above 600C,
(2) an X-ray powder diffraction pattern showing. inter
alia, the reflections given in Table A.
Table A
Radiation, Cu-K~ Wavelength 0.15418 nm
2 a relative intensity
_ _ _ _
7.~- 8.2 S
8.7- 9.1 M
11.8-12.1 W
12.4-12.7 W
10 14.6-lLI.9 W
15.4-15.7 W
15.8-16.1 W
17.6-17.9 W
19.2-19.5 W
20.2-20.6 W
20.7-21.1 W
23.1-23.4 VS
23.8-24.1 VS
24.;'-24.8 S
20 29.'7-30.1 M
__ .
where the letters used have the following meanings:
VS = very strong; S=strong; M=moderate; W=weak;
~ = ang1e according to Bragg's law.
(3) after evacuation at 2x 10 9 bar and 400C for
16 hours and measured at a hydrocarbon pressure
~lZ76'7~3
of 8x10 2 bar and 100C, the adsorption of
n-hexane is at least 0.8 mmol/g. the adsorption
of 2,2-dimethylbutane at least 0.5 mmol/g and the
ratio
adsorption of n-hexane
adsorption of 2,2-dimethylbutane at least 1.5.
(4) the composition, expressed in moles of the oxides,
is as follows
_ 3) M20- y(a Fe203- ~ A1203). SiO2
where
M - H and alkali metal
a ~ b = 1,
a ~ 0,
b ~ 0, and
0 < y ~ 0.1
Then, from the aromatic hydrocarbon mixture thus
obtalned a gaseous fraction containing propane and/or
butane and a liquid fraction boiling in the gasoline range
should be separated. Next, the gaseous fraction should
be subjected to partial dehydrogenation or partial oxida-
tion. Subsequently the o]efinic or oxygen-containing product
thus obtained is converted into an aromatic hydrocarbon
mixture using a crystalline silicate as defined above
as the catalyst. Finally, a fraction boiling in the gasoline
range is separated from the last-mentioned aromatic hydro-
carbon m;xture.
The present patent application therefore relates
o
to a process for the preparation of a hydrocarbon mixture
boiling in the gasoline range from a mixture of carbon
monoxide and hydrogen, in which
(a) the mixture of carbon monoxide and hydrogen is
converted into an aromatic hydrocarbon mixture using
a catalyst which contains a crystal]ine silicate
as defined hereinbefore,
(b) from the aromatic hydrocarbon mixture a gaseous fraction
containlng propane and/or butane and a liquid fraction
boiling in the gasoline range are separated,
(c) the gaseous fraction is subjected to partial dehydrogen-
ation or partial oxidation,
(d) the olefinic or oxygen-containing product obtained
according to (c) is converted into an aromatic hydrocarbon
mixture boiling in the gasoline range using a crystalline
silicate as defined hereinbefore as the catalyst, and
(e) from the aromatic hydrocarbon mixture obtained
accor-ding to (d) a fraction boiling in the gasoline
range is separated
The process according to the invention starts from
an H2/C0 mixture. Such a mixture may conveniently be
prepared by steam gasification of a carbon-containing
material. Examples of such materials are brown coal,
anthracite, coke, crude mineral oil and fractions there-
of, and oils recovered from tar sand and bituminous shale.
~12'^~670
--6--
The steam gasiflcation is prefer2bly carried out at a
temperature between 1000 and 2~00C and a pressure between
10 and 50 bar. In the process according to the invention
the preferred starting material is an H2/C0 mixture whose
molar ratio is between 0.25 and 1Ø
The H2/C0 mixture is converted in step (a) of the
process into an aromatic hydrocarbon mixture using a
catalyst which contains a crystalline silicate belonging
to a special class. A]though in steps (a) and (d) of the
process silicates may be used which contain both iron
and aluminium (a > 0 and b > 0), preference is given to
the use of silicates which contain either iron only
(a=1 and b=0) or aluminium only (a=0 and b=1). Step (a)
may in itself be carried out as a one-step or a two-step
process. In the two-step process the H2/C0 mixture is
preferab:Ly contacted in the first step with a catalyst
which contains one or more metal components having càtalytic
activity for the conversion of an H2/C0 mixture into
acyclic hydrocarbons. In the second step the product
thus obtained is converted into an aromatic hydrocarbon
mixture by contacting it under aromatization conditions
with the crystalline si~icate. In the one-step process
the H2/C0 mixture is contacted with a bifunctiona]
catalyst which contains, in addition to the crystalline
silicate, one or more metal components having catalytic
llZ~76~)
activity for the conversion of an H2/C0 mixture into
acyc'ic hydrocarbons and/or oxygen-containing hydro-
carbons. Step (a) of the process according to the
invention is preferably carried out as a one-step process.
The process according to the invention starts from
an H2/C0 mixture whose H2/C0 molar ratio may vary within
wide l1mits. Before this mixture is converted according
to step (a), its H2/C0 molar ratio may also be changed
by addition of hydrogen or carbon monoxide. The hydrogen
content of the mixture may be increased by subjecting
the mixture to the known water-gas shift reaction. If
the H2/C0 mixture that is used in the process as the feed
for step (a) has an H2/C0 molar ratio of less than 1,0,
step (a) is preferably carried out using a catalyst which
contains one or more metal components having catalytic
acitlvity for the water-gas shift reaction. When step (a)
is carried out as a two-step process, the H2/C0 mixture
with an H2/C0 molar ratio Or 1ess than 1.0 is preferably
contacted in the ri rst step with a bifunctional catalyst
which contains one or more metal components having catalytic
activity for the conversion of an H2/C0 mixture into
acyclic hydrocarbons and one or more metal components
having catalytic activity for the water-gas shift reaction
and the product thus obtained ;s converted in the second
step into an aromatic hydrocarbon mixture by contacting
it under aromatization conditions with the crystalline
~lZ7~7(~
silicate. ~hen s'ep (a) is carried out as a one-step process,
the H2/C0 mixture with an H2/C0 mo].ar ratio of less than
1.0 is preferably contacted with a trifunctional catalyst
which contains one or more metal components having catalytic
activity for the conversion of an H2/C0 mixture into acyclic
hydrocarbons and/or oxygen-containing hydrocarbons, one
or more metal. components having catalytic activity for
the water-gas shift reaction and the crystalline silicate.
Although the trifunctional catalysts which may be
used in step (a) of the process are described in this
patent application as catalysts which contain one or
more metal components having catalytic activity for the
conversion of an H2/C0 m~xture into acyclic hydrocarbons
and/or oxyeen-containing hydrocarbons, and one or more
metal components having catalytic activity for the wa-
ter-gas .shift reaction, this does not mean that separate
metal components which each have one Or the two catalytic
functions should always be present in the cata]ysts,
since it has been found that metal components and combi-
nations of metal components having catalytic activityfor the conversion of an H2/C0 mixture into substantially
oxygen-containing hydrocarbons have, as a rule~ also
sufficient catalytic activity for the water-gas shift
reaction, so that incorporation of one metal component
or one combination of metal components into the cata].ysts
~12~7~)
,: 'l suff ce. Exam~les of such metal components are the
metals chosen from the group formed by zinc, copper and
chromium. When trifunctional catalysts which contain
these metals are used in step (a) of the process, a tri-
functional catalyst is preferred which contains, in additionto the crystalline silicate, the metal combination zinc-
chromium. Metal components and metal combinations of metal
components having catalytic activity for the conversion
of an H2/C0 mixture into substantia]ly hydrocarbons have
as a rule no or insufficient activity for the water-gas
shift reaction. When such metal components or combinations
of metal components are used in the catalyst for the
first step of the two-step process or in the catalyst
for the one-step process, it will therefore be preferred,
when using feeds with an H2/C0 molar ratio of less than
1.0, to incorporate one or more separate metal components
having catalytic activity for the water-gas shift reaction
into the catalyst.
When an H2/C0 mixture with an H2/C0 mo]ar ratio of
less than 1.0 is used as the feed for step (a) of the
process, this step is preferably carried out as a one-step
process using a trifunctional catalyst which is composed
of two or three separate cata]ysts, wh~ch, for the sake
of con~enience, w-ll be designated catalysts X, Y and Z.
Catalyst X is the one which contains the metal components
llZ~7~
- 1 0 -
having ca~alytic ac'ivity for the conversion of an H2/C0
mixture into acyclic hydrocarbons and/or oxygen-containing
hydrocarbons. Catalyst Y is the crystalline silicate.
Catalyst Z is the one which contains the metal components
having catalytic activity for the water-gas shift reaction.
As explained hereinbefore, the use of a Z-catalyst may
in certain cases not be necessary.
If as the X-catalyst a catalyst is used which is
capable of converting an H2/C0 mixture into substantially
o~y~en-containing hydrocarbons, it is preferred to choose
a catalyst which is capable of converting the H2/C0 mixture
into substantially methano] and/or dimethyl ether. For
the conversion of an H2/C0 mixture into substantial1y
methano~, catalysts containing the above-mentioned metal
combinations (chosen from the group consisting of Cu,
Zn or Cr) are very suitable. X-catalysts which are capable
of converting an H2/C0 mixture into substantia1ly acyclic
hydrocarbons are known in the ~iterature as Fischer-Tropsch
catalysts. Such cataly3ts often contain one or- more metals
from the iron group or ruthenium together with one or more
promotors to increase the activity and/or selectivity.
If in step (a) of the process according to the invention
use is made of a catalyst combination in which catalyst X
is a Fischer-Tropsch catalyst, it is preferred to choose
for this purpose an iron or cobalt catalyst, in particu1ar
such a catalyst whjch has been preparec? by impregnation.
67C)
If desire~, it is also possible to use in step (a) of
the process according to the invention catalyst combina-
tions which contain a catalyst X which is capable of
converting an H2/C0 mixture into a mixture which contains
both hydrocarbons and oxygen-containing hydrocarbons in
comparable quantities. As a rule, such a catalyst also
has sufficient catalytic activity for the water-gas shift
reaction, so that the use of a catalyst Z in the combina-
tion can be omitted. An example of an X~catalyst of this
type is an iron/chromium oxide catalyst.
Z-catalysts which are capable of converting an H20/C0
mixture into an H2/C02 mixture are referred to in the
literature as C0-shift catalysts. If a Z-catalyst is used
in step (a) of the process accordjng to the invention,
it is preferred to choose for thls purpose a cata~yst
which contains the metal combination copper-zinc.
The trifunctional cata]ysts are preferably used as
a mixture. This mixture may be a macromixture or a mlcro-
mixture. In the first case the trjfunctional cata]yst
consists of two or three kinds of macroparticles, of
which one kind consists comp~etely of catalyst X, the second
kind completely of catalyst Y and the third kind, if present,
complete]y of catalyst Z. In the second case the trifunctional
catalyst consists of one kind of macroparticles, each
macroparticle being bui]t up of a great number of mi cro-
particles of each of the catalysts X, Y and, optional~y,Z.
67(~
-12-
In step (a) of the process it is preferred to use tri.-
functional catalysts in the form of micromixtures.
The crystalline silicate that is used in step (a)
and step (d) of the process is defined, inter alia. wlth
reference to the X-ray powder diffraction pattern of the
silicate after 1 hour's calcining in air at 500C. This
X-ray powder diffraction pattern should show, inter a]ia,
the reflections given in Table A. The complete X-ray powder
diffraction pattern of a typi.cal example of a silicate
eli~ible for use according to the invention is shown in
Table B (Radiafion: Cu-K~ ; wavelength: 0.15418 nm).
T _ e B
2 0 relative intensity description
(100.I/Io)
_ _ _
8.00 55 SP
8.90 36 SP
9.10 20 SR
11.95 7 NL.
12.55 3 NL
13.25 4 NL
13.95 10 NL
14.75 9 BD
15.55 7 BD
9 BD
17.75 5 BD
19.35 6 NL
670
~0.40 ~ ~TL
20.90 10 NL
21.80 4 NL
22.25 8 NL
23.25 100X) SP
23.95 ~5 SP
24.40 27 SP
25.90 11 BD
26.70 9 BD
27.50 4 NL
29.30 7 NL
29.90 11 BD
31.25 2 NL
32.75 4 NL
34.40 4 NL
36.05 5 BD
37.50 4 BD
45.30 9 BD
x) Io = intensity of the 3trongest separate reflection
present in the pattern.
The letters used in Table B for describing the ref].ections
have the follow.ing meanings:
SP = sharp; SR = shoulder; NL = normal; BD = broad;
~ = angle according to Bragg's law.
The crystal].ine silicates may be prepared from an
aqueous mixture as the starting materia~ which contains
~lZ76'7
- 1 4 -
the following compounds in a given ratio: one or more
compounds of an alkali metal (M~, one or more compounds
containing an organic cation (R) or from which such a cation
is formed during the preparation of the silicate, one
or more silicon compounds and one or more a]uminium and/or
iron compounds. The preparation is performed by maintaining
the mixture at elevated temperature until the silicate
has been formed and subsequently separating the crystals
of the silicate from the mother liquor. In the preparation
of the silicates it is preferred to start from a base
mixture in which M is present in a sodium compound and
R in a tetrapropylammonium compound.
The silicates prepared as described above contain
alkali metal ions and organic cations. When suitable
exchange methods are used, the alka]i metal ions can be
replaced by other cations, such as hydrogen ions or
ammonium ions. Organic cations can very convenient1y be
converted into hydrogen ions by calcin;ng the silicates.
The crystalline silicates which are used in the catalysts
preferably have an alka]i metal content of less than 1 %w,
and in particular Or less than 0.05 %w.
Step (a) of the process is preferably carried out at
a temperature of 200-500C and in particular of 300-450C,
a pressure of 1-50 bar and in particular of 5-100 bar
and a space velocity of 50-5000 and in particular of
300-3000 Nl gas/l catalyst/h.
llZ7670
-15-
Ste? (a~ of the process can very conveniently be
carried out by conducting the feed in upward or downward
direction through a vertical~y mounted reactor in which
a fixed or a moving catalyst bed is present. Step (a)
of the process may, for instance, be carried out by
conducting the feed in upward direction through a vertically
mounted catalyst bed, at such a gas rate that expansion
of the catalyst bed takes place. If desired, step (a)
of the process may a~so be carried out using a suspension
0 of the catalyst in a hydrocarbon oil. Depending on whether
step (a) of the process is carried out with a fixed cata-
lyst bed, an expanded catalyst bed or a catalyst suspension,
preference is given to catalyst particles with a diameter
between 1 and 5 mm, 0.5 and 2.5 mm and 20 and 150~ m,
respectively.
From the aromatic hydrocarbon mixture obtained according
to step (a), a ga~seous fraction containing propane and/or
butane and a liquid fraction boiling in the gasoline range
should, according to the invention, be separated jn step (b).
Preferably the reaction mixture originating from step (a)
is separated in step (b) into a C2 fraction, a C3/C4 fraction
and a C5+ gasoline fraction. The C2 fraction may be used
as fuel gas. If desired, from the C2 fraction an H2/C0
mixture may be separated, which may be recycled to step (a).
If the hydrocarbon content of the C2- fraction is suffi-
1~2767~)
-- 1 6--
cient1y high, it may be preferable to subject this fraction,
either w.th an ,~2/C0 mixture present or after its removal,
to steam reforming in order to prepare additional synthesis
gas which can be used as feed component for step (a).
The steam reforming of the C2 fract;on may very conve-
niently be effected by contacting this fraction together
with steam at elevated temperature and pressure with a
nickel-containing catalyst.
In the process according to the invention the gaseous
fraction containing propane and/or butane should be subjected
in step (c) to partial dehydrogenation or partial oxidation.
Partia] dehydrogenation of the gaseous fraction may be
effected by contacting this fraction at elevated temperature
with a chromium-containing catalyst. Partial oxidation
of the gaseous fraction may be effected by treating the
fraction, optionally in the presence of a catalyst, at
elevated temperature with a less than theoretical quantity
of oxygen. As a rule, in the partial oxidation C0 is
formed, which may be used, lf desired, as feed component
for step (a~.
In the process according to the invention the olefinic
or oxygen-containing product obtained according to step (c~
should be converted in step (d~ into an aromatic hydrocarbon
mixture by contacting it under aromatization conditions
with a silicate as defined hereinbefore. From the product
prepared according to step (d) a fraction bolling in the
~Z767(~
-17-
gasoline range is separated in step (e).
The conversion of the olefinic or oxygen-containing
product obtained according to step (c) over the crystalline
silicate may, in principle, be effected in two ways. The
product prepared according to step (c) may be contacted
in a separate reactor with the crystal]ine silicate or,
alternatively, if step (a) of the process according to
the invention is carried out as a two-step process, the
product prepared according to step (c) can very conveniently
be mixed with the product o~ the first step.
An attractive embodiment of the process according to
the invention is one in wh;ch the conversion of the product
prepared according to step (c) is carried out by contacting
this product in step (d) in a separate reactor with the
crystalline silicate, separating from the product prepared
according to step (d) a gaseous fraction containing propane
and/or butane and a liquid fraction boi]ing i.n the gasollne
ran~e, and recycling the easeous fraction to step (c).
A process scheme for the conversion of synthesis gas
into aromatic gasoline according to the invention wlll be
explained below in more detai.l with reference to the drawing.
P_ocess scheme (see figure)
The process is carried out in an apparatus which
comprises, in succession, a methanol synthesis unit (1),
an aromatization unit (2), a separation unit (3), a partial
7~
oxidation unit (4), another aromatization unit (5) and
another separation unit (6). An H2/CO mixture (7) i.s converted
into methanol (8). The methanol stream is divided into
two portions (9) and (10). Portion (9) is aromatized. The
aromatized product (10) is separated into a C2 fraction (11),
a C3/C4 fraction (12) and a C5T gasoline fraction (13).
The C3/C4 fraction (12) is mixed with a C3tC4 fraction (14)
and the mlxture (15) is partially oxidized. The partia~.l.y
oxidized product (16) is mi.xed with methano] portion (10)~
and the mi.xture (17) is aromatized. The aromatized product (18)
is separated into a C2 fraction (19), a C3/C4 fraction (14)
and a C5+ gasoline fraction (20).
The present patent application also comprises an
apparatus for carrying out a process according to the inven-
tion as shown schematically in the figure.
The invention will now be explained with referenceto the following example.
EXAMPEE
A crystall.ine silicate (silicate A) was prepared as
follows. A mixture of SiO2, Fe(N03)3, NaOH and /TC3H7)4N70H
in water with the mol.ar composition
8 Na20.Fe203. 12/~C3H7)4N72o. 200 SiO2. 3750 H20 was heated
for 48 hours in an autoc]ave at 150C under autogenous
pressure. After the reaction mixture had cooled down, the
silicate formed was filtered off, washed with water until
the pH of the wash water was about 8 and dried for two hours
67()
,9
at 120C. After 1 hour's ca]clning in air at 500C s;licate A
had the following properties:
(a) thermally stable up to a temperature above 900C
(b) an X-ray powder diffraction pattern substantially
equal to the one given in Table B.
(c) after evacuation for 16 hours at 2xlO 9 bar and 400C
and measured at a hydrocarbon pressure of 8x10 2 bar
and 100C, the adsorption of n-hexane is 1.2 mmol/g.
the adsorption of 2,2-dimethylbutane 0.7 mmol/g and
l the ratio
adsorption of n-hexane
adsorption of 2,2-dimethylbutane 1-7~ and
(d) the composition, expressed in moles of the oxides,
is 0.0054 M20. 0.0054 Fe203. SiO2, where M=H and Na.
From silicate A, which had an average crystallite
size of 225 nm, a silicate B was prepared by boi]ing the
material calcined at 500C with 1.0 molar NH4N03 solution,
washing with water, bo~line again with l.0 molar NH4N03
solution and wa~hing, drying for 2 hours at 120C and
calcining for 1 hour at 500C.
A crystalline silicate (silicate C) was prepared
in substantially the same way as silicate A, the difference
being that for the preparation of sillcate C the starting
material was an aqueous mixture which contained Na2AlO2
instead of Fe(N03)3 and which had the following molar
composition:
6~V
2 .Fe203- 72[(C3~17)4N]20- 400 si~2 7200 H20-
After I hour's calcining in air at 500C silicate C was
completely identical to silicate A as regards X--ray powder
diffraction pattern and adsorption behaviour.
Silicate C was thermally stable up to a temperature above
800C. The composition of silicate C ~after calcining),
expressed in moles of the oxides, was as follows:
0-0035 M20. 0.0035 A1203.SiO2, where M=l-l and Na.
From silicate C, which had an average crystallite
size of 240 nm, a silicate D was prepared in the same
way as described above for the preparation of s;licate B
from sil-icate ~.
Iwo catalyst mixtures (I and II~ were prepared by
mixing a ZnO~Cr203 composition with silicate B and with
silicate D~ respectively. The atomic Zn percentage o~
the ZnO-Cr203 composition based on the sum of Zn and Cr
was 70%. Tlle catalyst mixtures both contained per part
by volume of silicate, 2 parts by volume of the ZnO-Cr203
composition.
('atalyst nliXtllroS I (l~rol1are(l with silic.lto 1~) alld
II (proparod with silicato 1)) were used in a l~rocess for
the preI)aration of an aromatic hydrocarbon mixture boiling
:in tl~e gaselirle rallgo, witl- an ll2/CO mixture with an
112/C0 molilr ratio of 0.5 as the starting material. To
this end the 112/C0 mixture was converte{l in one step into
an aromatic hydrocarbon rnixture by conducting it at a
- 20 -
~'
67~3
-21-
temperature of 375C, a pressure of 60 bar and a space
velocity of 200 1.l 1.h 1 over a fixed bed with a volume
of 7.5 ml of the catalyst mixture concerned, wh;ch was
present in a 50-ml reactor. The product thus obtained
was separated into a C2 fraction, a C3/C4 fraction and
a C5 gasoline fraction. The C3/C4 fraction was partially
dehydrogenated and the product thus obtained was aromatized
- by contacting it at a temperature of 375C, a pressure
of 3~ bar and a space velocity at 2 kg.kg l.h 1 with
silicate B or silicate D. The product thus obtained was
separated into a C4 fraction and a C5~ gasoline fraction.
The resu]ts of these experiments are given below.
6~
-22-
E~periment No - 1 2
Conversion of the H /C0 mixture
2~
carried out using cat_lyst
mixture No. I II
C position of the aromatic_ _ _
hydrocarbon mixture prepar__
from t_e H2/C0 mixture (C1+),%w
C2 10 7
c3/c4 26 32
C5 64 61
Comp_sition of the C5+fraction,
prepared from the H2/C0
mixture, %w
acyclic hydrocarbons 20 18
15 naphthenes 18 16
aromatics 62 66
Average conversion of
C3/C4 paraffins into
C3/C4 l_fins, % 33 34
Aromatiz_tlon of the partia]ly
dehydrogenated C3/C4 fractio_
carried out using silicate No. B D
Yield of C +fraction, calcula-
--5
ted on C1~, %w 6 8
Aromatics con_ent of the
last_mentlone_ C5+fraction. ~_ 85 88
