U.S. patent application number 11/840870 was filed with the patent office on 2008-02-21 for method and apparatus for steam dealkylation in a plant for the catalytic reforming of hydrocarbons.
This patent application is currently assigned to Linde Aktiengesellschaft. Invention is credited to Helmut Fritz, Volker Goeke.
Application Number | 20080041763 11/840870 |
Document ID | / |
Family ID | 38954984 |
Filed Date | 2008-02-21 |
United States Patent
Application |
20080041763 |
Kind Code |
A1 |
Fritz; Helmut ; et
al. |
February 21, 2008 |
METHOD AND APPARATUS FOR STEAM DEALKYLATION IN A PLANT FOR THE
CATALYTIC REFORMING OF HYDROCARBONS
Abstract
A method and apparatus for treating a fraction consisting
predominantly of hydrocarbons having at least six carbon atoms
(C.sub.6+ fraction) as produced in a plant for the catalytic
reforming of hydrocarbon-containing feedstock, is disclosed. The
C.sub.6+ fraction is taken for steam dealkylation where the useable
products benzene and hydrogen are produced.
Inventors: |
Fritz; Helmut; (Muenchen,
DE) ; Goeke; Volker; (Wolfratshausen, DE) |
Correspondence
Address: |
CROWELL & MORING LLP;INTELLECTUAL PROPERTY GROUP
P.O. BOX 14300
WASHINGTON
DC
20044-4300
US
|
Assignee: |
Linde Aktiengesellschaft
Abraham-Lincoln-Strasse 21
Wiesbaden
DE
65189
|
Family ID: |
38954984 |
Appl. No.: |
11/840870 |
Filed: |
August 17, 2007 |
Current U.S.
Class: |
208/56 ; 208/57;
208/66; 422/202 |
Current CPC
Class: |
C01B 2203/043 20130101;
C01B 2203/148 20130101; C01B 2203/1252 20130101; C01B 3/56
20130101; C01B 3/384 20130101; C10G 2400/26 20130101; C01B
2203/0855 20130101; C01B 2203/1064 20130101; C01B 2203/1247
20130101; C01B 2203/0866 20130101; C07C 2521/04 20130101; C07C
2523/46 20130101; C07C 2521/10 20130101; C01B 2203/0233 20130101;
C07C 4/20 20130101; C07C 2523/44 20130101; B01J 8/062 20130101;
C07C 4/20 20130101; C01B 2203/048 20130101; C01B 2203/0811
20130101; C07C 2523/26 20130101; C01B 2203/047 20130101; C01B
2203/0475 20130101; C01B 2203/1258 20130101; C01B 2203/1082
20130101; C10G 2400/30 20130101; C07C 15/04 20130101 |
Class at
Publication: |
208/056 ;
208/057; 208/066; 422/202 |
International
Class: |
C10G 45/08 20060101
C10G045/08 |
Foreign Application Data
Date |
Code |
Application Number |
Aug 18, 2006 |
DE |
10 2006 038 892.5 |
Dec 12, 2006 |
DE |
10 2006 058 534.8 |
Claims
1. A method for treating a fraction consisting predominantly of
hydrocarbons having at least six carbon atoms (C.sub.6+ fraction)
as produced in a plant for catalytic reforming of
hydrocarbon-containing feedstock, wherein the C.sub.6+ fraction
undergoes steam dealkylation, where two usable product materials
benzene and hydrogen are produced in addition to reaction products
such as carbon monoxide and carbon dioxide.
2. The method according to claim 1, wherein the C.sub.6+ fraction
contains: a) aromatic hydrocarbons having six to ten carbon atoms;
b) cyclic paraffins (cycloalkenes) having five to ten carbon atoms;
c) iso- and n-paraffins having five to ten carbon atoms; d) alkenes
having six to ten carbon atoms; or any mixture of the
aforementioned.
3. The method according to claim 1, wherein the hydrocarbons from
the C.sub.6+ fraction react with water in a gas phase with addition
of heat to a solid catalyst.
4. The method according to claim 1, wherein heat required for the
dealkylation reaction is generated by combustion of a starting
material with air.
5. The method according to claim 1, wherein gaseous reaction
products from the steam dealkylation are separated following
compression by way of pressure swing adsorption into gaseous
hydrogen and gaseous reaction by-products, specifically carbon
monoxide, carbon dioxide and methane.
6. The method according to claim 5, wherein the gaseous reaction
by-products from the steam dealkylation, specifically carbon
monoxide and methane, are used as starting material for the
combustion with air.
7. The method according to claim 1, wherein flue gases generated
during combustion are cooled by a heat exchanger while heating
starting materials for the steam dealkylation.
8. The method according to claim 1, wherein the C.sub.6+ fraction
and the steam are conducted in pipes, from top to bottom, past a
solid catalyst, where the catalyst is on an inside of the
pipes.
9. The method according to claim 8, wherein heat is brought to the
pipes from outside.
10. The method according to claim 9, wherein the heat required for
the dealkylation reaction is transferred to the pipes by
electromagnetic radiation, thermal radiation and/or convection.
11. The method according to claim 1, wherein a solid catalyst of a
porous carrier material is used, specifically
.gamma.-Al.sub.2O.sub.3, MgAl spinel and/or Cr.sub.2O.sub.3 and an
active component on a surface of the carrier material, in
particular Rh with 0.1-1.0% loading by weight and/or Pd with
0.2.-2.0% loading by weight.
12. The method according to claim 1, wherein the steam dealkylation
is performed at a temperature of 400.degree. C. to 600.degree. C.,
preferably 450.degree. C. to 550.degree. C., particularly
preferably 480.degree. C. to 520.degree. C.
13. The method according to claim 1, wherein the steam dealkylation
is performed at a pressure from 1 to 15 bar, preferably 1.2 to 10
bar, particularly preferably 1.5 to 8 bar.
14. The method according to claim 1, wherein the steam dealkylation
is performed at a molar quotient of steam to hydrocarbons in a
range from 1 to 20, preferably from 2 to 15, when it enters a
reactor.
15. The method according to claim 1, wherein the steam dealkylation
is performed at a molar quotient of steam to hydrocarbons which is
in a range from 3 to 12, preferably from 5 to 10, when it enters a
reactor.
16. The method according to claim 1, wherein the C.sub.6+ fraction
undergoes a process prior to the steam dealkylation to convert
dienes and styrenes where in particular hydrating methods are
employed involving consumption of hydrogen.
17. The method according to claim 1, wherein the C.sub.6+ fraction
undergoes a process prior to the steam dealkylation to convert and
to remove components containing sulfur, nitrogen and/or oxygen, in
which specifically hydrating processes involving consumption of
hydrogen are employed.
18. The method according to claim 1, wherein the reaction products
from the steam dealkylation are cooled and separated into gaseous
reaction products, hydrocarbons and water in a 3-phase
separation.
19. The method according to claim 16, wherein the hydrogen produced
in the steam dealkylation of the C.sub.6+ fraction is fed
completely or partially into a starting material for the processes
involving the consumption of hydrogen.
20. The method according to claim 17, wherein the hydrogen produced
in the steam dealkylation of the C.sub.6+ fraction is fed
completely or partially into a starting material for the processes
involving the consumption of hydrogen.
21. The method according to claim 1, wherein the hydrogen produced
in the steam dealkylation of the C.sub.6+ fraction is fed as
starting material to a process consuming hydrogen in an oil
refinery, preferably into a process to convert and remove
components containing sulfur or a process to split
hydrocarbon-containing starting material via hydrogen.
22. The method according to claim 1, wherein a sulfur content in
the C.sub.6+ fraction is reduced to below 10 ppm, preferably below
3 ppm, particularly preferably below 1 ppm prior to the steam
dealkylation.
23. The method according to claim 1, wherein the benzene is
separated from the hydrocarbons by way of rectification of the
reaction products.
24. The method according to claim 23, wherein the benzene undergoes
adsorptive fine cleaning following rectification to dry and remove
trace components, where the benzene is passed across an adsorbent
on which the trace components are adsorbed.
25. The method according to claim 1, wherein components boiling
close to benzene or forming azeotropes in the C.sub.6+ fraction are
converted by steam dealkylation.
26. The method according to claim 23, wherein all heavier boiling
reaction products than benzene from rectification, consisting
predominantly of non-converted feedstocks from the steam
dealkylation are returned to the steam dealkylation as feedstock
via optional hydration.
27. The method according to claim 23, wherein all heavier boiling
reaction products than benzene from rectification consisting
predominantly of non-converted feedstocks from the steam
dealkylation are returned prior to steam dealkylation for hydration
of the C.sub.6+ fraction or for hydration of a fraction consisting
predominantly of hydrocarbons having at least five carbon
atoms.
28. The method according to claim 1, wherein linear hydrocarbons
are separated from the C.sub.6+ fraction prior to steam
dealkylation by means of liquid-liquid extraction.
29. The method according to claim 1, wherein a fraction consisting
predominantly of hydrocarbons having at least eight carbon atoms
(C.sub.8+ fraction) is separated by distillation from the C.sub.6+
fraction prior to steam dealkylation where the C.sub.8+ fraction is
taken as feedstock to a process to extract paraxylene.
30. The method according to claim 29, wherein following separation
of the C.sub.8+ fraction, benzene is separated from the C.sub.6+
fraction prior to the steam dealkylation.
31. An apparatus for treating a fraction consisting predominantly
of hydrocarbons having at least six carbon atoms (C.sub.6+
fraction) as produced in a plant for catalytic reforming of
hydrocarbon-containing feedstock, wherein the apparatus includes an
oven with a furnace and pipes located in the furnace.
32. The apparatus according to claim 31, wherein the pipes are
mounted vertically in the furnace and have heat expansion
compensating elements at a lower and/or an upper end.
33. The apparatus according to claim 31, wherein each pipe has a
supply for the C.sub.6+ fraction and the steam and an outlet for
the reaction products.
34. The apparatus according to claim 31, wherein each pipe is
filled on an inside with a catalyst, where the catalyst consists of
a porous carrier material, specifically .gamma.-Al.sub.2O.sub.3,
MgAl spinel and/or Cr.sub.2O and an active component on a surface
of the carrier material, in particular Rh with 0.1-1.0% loading by
weight and/or Pd with 0.2.-2.0% loading by weight.
35. The apparatus according to claim 31, wherein the oven has at
least one burner on a wall, a ceiling and/or a floor.
36. The apparatus according to claim 31, wherein the pipes are
suitable for an internal pressure of 1 to 15 bar, preferably 1.2 to
10 bar, particularly preferably 1.5 to 8 bar, and for use in an
oven with flame temperatures of up to 1400.degree. C.
37. A method of extracting benzene from a hydrocarbon having at
least six carbon atoms, comprising the steps of: producing the
hydrocarbon having at least six carbon atoms in a plant for
catalytic reforming of hydrocarbon-containing feedstock; subjecting
the hydrocarbon having at least six carbon atoms to steam
dealkylation; and producing benzene from the steam
dealkylation.
38. The method according to claim 37, further comprising the step
of producing hydrogen from the steam dealkylation.
Description
[0001] This application claims the priority of German Patent
Documents No. 10 2006 038 892.5, filed Aug. 18, 2006, and No. 10
2006 058 534.8, filed Dec. 12, 2006, the disclosures of which are
expressly incorporated by reference herein.
BACKGROUND AND SUMMARY OF THE INVENTION
[0002] The invention relates to a method for treating a fraction
consisting predominantly of hydrocarbons having at least six carbon
atoms (C.sub.6+ fraction) as produced in a plant for the catalytic
reforming of hydrocarbon-containing starting material and an
apparatus to carry out the method.
[0003] Heavy naphtha is produced primarily in a plant for the
catalytic reforming of hydrocarbon-containing feedstock, such as is
produced, for example, in crude oil distillation.
[0004] The heavier naphtha such as is produced in crude oil
distillation, contains principally iso- and n-paraffins, napthenes
and aromatics having predominantly six to twelve carbon atoms,
where the percentage of aromatics may also be very low and depends
on the starting material. In the prior art, the heavier naphtha
first undergoes desulfurization in which hydrogen is consumed and
hydrogen sulfide is created and is then taken as starting material
to catalytic reforming. In the catalytic reforming, principally the
existing paraffins and napthenes are converted into aromatics in
the presence of a catalyst, where hydrogen and light hydrocarbons
are created/formed as by-products. These by-products are separated
from the reaction products of the catalytic reforming so that a
fraction consisting predominantly of hydrogen and hydrocarbons
having up to five carbon atoms and a fraction consisting
predominantly of hydrocarbons having at least six carbon atoms
(C.sub.6+ fraction) is produced. This C.sub.6+ fraction contains
aromatics as an economically usable product, primarily benzene,
which are used as starting material for the synthesis of numerous
plastics and to increase the knock resistance of gasoline.
[0005] In order to obtain the economically usable products from the
C.sub.6+ fraction, principally benzene, and to make the yield as
large as possible, the following method is used in accordance with
the prior art. By means of fluid-fluid extraction, the linear
hydrocarbons are separated and processed further as raffinate, for
example the raffinate can be returned to the starting material for
catalytic reforming. The C.sub.6+ fraction freed from the linear
hydrocarbons now contains primarily aromatics having six to eight
carbon atoms and is separated into a fraction consisting
predominantly of hydrocarbons having six or seven carbon atoms
(principally benzene and toluene) and into a fraction consisting
predominantly of hydrocarbons having eight carbon atoms (primarily
xylene). The fraction consisting predominantly of hydrocarbons
having at least eight carbon atoms is taken as starting material to
a process for extracting para-xylene. Benzene is extracted from the
fraction consisting predominantly of hydrocarbons having six or
seven carbon atoms before this fraction is taken as starting
material to a process for hydro-dealkylation.
[0006] A method of this kind for hydro-dealkylation is described,
for example, in WO2005071045. The hydrocarbons are contacted with
hydrogen in the presence of a catalyst at a temperature of
400.degree. C. to 600.degree. C. and a pressure between 20 bar and
40 bar, where the hydrogen is present in a molar excess of three to
six times the hydrocarbons. Under these conditions the alkyl groups
are split off from the specific alkylated aromatics (for example,
toluene or xylene) so that benzene and the specific alkanes (for
example, methane and ethane) form.
[0007] The consumption of hydrogen in the hydro-dealkylation of the
hydrocarbons has a negative effect on the economics of this method
from the prior art for extracting benzene.
BRIEF DESCRIPTION OF THE DRAWING
[0008] FIG. 1 illustrates an embodiment of an apparatus in
accordance with the principles of the present invention.
DETAILED DESCRIPTION OF THE EXEMPLARY EMBODIMENTS
[0009] In accordance with the invention, with respect to the
method, the C.sub.6+ fraction is subjected to steam dealkyation
where mainly the two utilizable products benzene and hydrogen are
produced along with reaction products such as carbon monoxide and
carbon dioxide.
[0010] The basic idea of the invention is to carry out the
dealkylation of the alkylated aromatics while generating benzene
with the aid of steam dealkylation. Steam dealkylation requires
only low-cost steam as the starting material and produces the
valuable by-product hydrogen in addition to the desired quality
product benzene.
[0011] The C.sub.6+ fraction used in the steam dealkylation
contains primarily: [0012] a) aromatic hydrocarbons having six to
ten carbon atoms, [0013] b) cyclic paraffins (cycloalkenes) having
five to ten carbon atoms, [0014] c) iso- and n-paraffins having
five to ten carbon atoms, [0015] d) alkenes having six to ten
carbon atoms, or any mixture of the preceding, in which the exact
composition of the mixture depends on the composition of the
specific heavier naphtha which is taken as starting material for
catalytic reforming. The method in accordance with the invention is
suitable for each of the compounds of the C.sub.6+ fractions
described.
[0016] The hydrocarbons from the C.sub.6+ fraction advantageously
react with steam in the gas phase with the introduction of heat on
a solid catalyst. The gaseous C.sub.6+ fraction is dealkylated by
the presence of gaseous water (steam) on a catalyst with the
constant introduction of heat, whereby the desired products benzene
and hydrogen are produced in addition to carbon monoxide, carbon
dioxide and additional by-products.
[0017] Preferably the heat required for the dealkylation reaction
is generated from combustion of a starting material with air. It
proves to be particularly advantageous to use gaseous reaction
by-products from the steam dealkylation, specifically carbon
monoxide and methane as the starting material for combustion with
air. A part of the gaseous reaction by-products from the steam
dealkylation, in particular carbon monoxide and methane, is
combustible and can thus serve as starting material for combustion
to generate the required reaction heat. This saves heating gas and
this otherwise unused part of the reaction products is employed
usefully.
[0018] The gaseous reaction products, following compression, are
expediently separated by way of pressure swing adsorption into
gaseous hydrogen and gaseous reaction by-products, specifically
carbon monoxide, carbon dioxide and methane. The valuable
by-product hydrogen is also present in gaseous form and can be
employed much more usefully than in combustion. By means of
pressure swing adsorption with prior compression, the hydrogen can
easily be separated from the combustible gaseous reaction
by-products which can serve as starting material in the
combustion.
[0019] The flue gases generated during combustion are
advantageously cooled by means of a heat exchanger while heating
the starting materials for steam dealkylation. By using the heat of
the flue gases to pre-heat the starting materials (C.sub.6+
fraction and steam) for steam dealkylation, the heat that has to be
brought in to maintain the required temperatures for the steam
dealkylation is reduced. This achieves an economical use of energy
resources.
[0020] The C.sub.6+ fraction and the steam are advantageously taken
past the solid catalyst in pipes, preferably from top to bottom,
with the catalyst being located inside the pipes. Heat is
expediently brought to the pipes from the outside. The heat
required for the dealkylation reaction is advantageously
transferred to the pipe by electromagnetic radiation, thermal
radiation and/or convection. The actual dealkylation reaction takes
place inside the pipes where the catalyst is located. The two
components in the reaction (C.sub.6+ fraction and steam) are taken
from top to bottom through the pipes filled with the catalyst. The
heat required for the dealkylation reaction is generated outside
the pipes and transferred to the pipe by the mechanisms named from
which the heat is transferred by means of conduction and convection
into the interior of the pipes where the reaction is taking
place.
[0021] Preferably a solid catalyst of a porous carrier material is
used, in particular .gamma.-Al.sub.2O.sub.3, MgAl spinel and/or
Cr.sub.2O.sub.3, and an active component on the surface of the
carrier material, in particular Rh with 0.1-1.0% loading by weight
and/or Pd with 0.2-2.0% loading by weight.
[0022] The steam dealkylation is advantageously performed at a
temperature of 400.degree. C. to 600.degree. C., preferably
450.degree. C. to 550.degree. C., particularly preferably
480.degree. C. to 520.degree. C. and at a pressure of 1 to 15 bar,
preferably 1.2 to 10 bar, particularly preferably 1.5 to 8 bar.
[0023] The steam dealkylation is expediently performed at a molar
quotient of steam to hydrocarbons which lies in the range from 1 to
20, preferably from 2 to 15, when it enters the reactor. In another
embodiment of the invention, the steam dealkylation is performed at
a molar quotient of steam to hydrocarbons which lies in the range
from 3 to 12, preferably from 5 to 10 when it enters the reactor.
Generally the steam dealkylation is performed with a molar excess
of water, where the exact ratio in the different embodiments of the
inventions depends on the precise composition of the C.sub.6+
fraction.
[0024] It proves advantageous to subject the C.sub.6+ fraction
before steam dealkylation to a process to convert dienes and
styrenes, where specifically hydrating methods consuming hydrogen
are employed. In another embodiment of the invention, the C.sub.6+
fraction is separated before steam dealkylation from a fraction of
hydrocarbons having at least six carbon atoms where the fraction of
hydrocarbons having at least six carbon atoms is subjected to a
process to convert dienes and styrenes, specifically a hydrating
process which consumes hydrogen. By employing the hydrating
methods, any diolefins present in the C.sub.6+ fraction are
converted into their corresponding olefins, just as components
containing sulfur, nitrogen and oxygen can be converted and
removed. Deactivation of the catalyst is reduced and the life of
the catalyst is clearly increased.
[0025] The reaction products from the steam dealkylation are
preferably cooled and separated in a 3-phase separation into
gaseous reaction products, hydrocarbons and water. The reaction
products coming from the steam dealkylation contain not only the
desired quality products benzene and hydrogen but also reaction
products such as carbon monoxide and carbon dioxide and reaction
by-products. To obtain the desired quality products, the reaction
products must be separated. This is done by way of a 3-phase
separation of the cooled reaction products into gaseous reaction
products, in particular hydrogen, carbon monoxide, carbon dioxide
and methane, into hydrocarbons, in particular benzene, and into
water.
[0026] The hydrogen generated in the steam dealkylation of the
C.sub.6+ fraction is expediently fed completely or partially into
the starting material for the hydrogen-consuming processes. The
hydrogen generated in the steam dealkylation can be used entirely
or partially for the hydrogen-consuming processes described in the
previous section so that the need for hydrogen to be supplied
externally is minimized.
[0027] In a further embodiment of the invention the hydrogen
produced in the steam dealkylation of the C.sub.6+ fraction is
taken as starting material to any process consuming hydrogen in the
oil refinery, preferably to a process for converting and removing
sulfur-containing components or to a process for reforming a
hydrocarbon-containing starting material by means of hydrogen.
[0028] Reduction of the sulfur content in the C.sub.6+ fraction to
below 10 ppm, preferably to below 3 ppm, particularly preferably to
below 1 ppm, before steam dealkylation proves advantageous for a
good yield of the desired reaction product benzene.
[0029] Preferably the benzene is separated from the hydrocarbons of
the reaction products through rectification. Following
rectification, the benzene advantageously undergoes adsorptive fine
cleaning to dry and remove the trace components, where the benzene
is directed across an adsorbent on which the trace components, as
opposed to benzene, are adsorbed. By applying the inventive
process, the benzene can be extracted from the reaction products by
simple rectification and processed further or marketed. Expensive
rectification or extra rectification as when applying a process in
accordance with the prior art is not necessary, thus reducing
investment and process costs.
[0030] Advantageously components boiling close to benzene or
components forming azeotropes in the C.sub.6+ fraction are
converted by the steam dealkylation. All reaction products boiling
heavier than benzene from rectification, consisting predominantly
of non-converted starting materials from the steam deakylation are
expediently returned to steam dealkylation through optional
hydration as starting material. In another embodiment of the
invention, all reaction products boiling heavier than benzene from
rectification, consisting predominantly of non-converted starting
materials from steam dealkylation are returned for hydration of the
C.sub.6+ fraction or hydration of a fraction consisting
predominantly of hydrocarbons having at least five carbon atoms
prior to steam dealkylation. By returning the non-converted
starting materials for hydration or for steam dealkylation,
circulation is achieved without losing valuable starting
materials.
[0031] In a further embodiment of the invention, the linear
hydrocarbons are separated from the C.sub.6+ fraction prior to
steam dealkylation by means of fluid-fluid extraction, whereby the
linear hydrocarbons are returned to the starting material for
catalytic reforming.
[0032] In another embodiment of the invention, prior to steam
dealkylation a fraction consisting predominantly of hydrocarbons
having at least eight carbon atoms (C.sub.8+ fraction) is separated
by distillation from the C.sub.6+ fraction, where the separated
C.sub.8+ fraction is taken to a process for extracting para-xylene
or gasoline. Following separation of the C.sub.8+ fraction, benzene
is advantageously separated from the C.sub.6+ fraction prior to the
steam dealkylation. Through the separation of the C.sub.8+ fraction
and the removal of benzene, the C.sub.6+ fraction now contains
predominantly toluene which is effectively converted into benzene
by the application of the method in accordance with the
invention.
[0033] Concerning the apparatus, the object of the invention is
achieved by the apparatus comprising an oven 100 with a furnace 110
and pipes 120 located in the furnace. The actual steam dealkylation
takes place in the pipes which in turn are located in the furnace
of the oven where the heat required for steam dealkylation can be
generated.
[0034] The pipes are advantageously installed vertically in the
furnace and have heat expansion compensating elements 130 at the
lower and/or upper end. The heat expansion compensating elements at
the lower and/or upper end of the vertical pipes prevent mechanical
stress from temperature differences which can lead to increased
wear of the pipes.
[0035] Each pipe expediently has a supply for the C.sub.6+ fraction
and the steam, 122, 124, respectively, and an outlet 126 for the
reaction products.
[0036] It similarly proves advantageous that each pipe is filled on
the inside with a catalyst, where the catalyst consists of a porous
carrier material, in particular .gamma.-Al.sub.2O.sub.3, MgAl
spinel and/or Cr.sub.2O.sub.3 and an active component on the
surface of the carrier material, in particular Rh with 0.1-1.0%
loading by weight and/or Pd with 0.2.-2.0% loading by weight.
[0037] Preferably the oven has at least one burner 102 on the wall,
the ceiling and/or the floor. The pipes are expediently suitable
for an internal pressure of 1 to 15 bar, preferably 1.2 to 10 bar,
particularly preferably 1.5 to 8 bar, and for use in an oven with
flame temperatures of up to 1400.degree. C.
[0038] The present invention is successful specifically in creating
an economical alternative to the prior art for treating a C.sub.6+
fraction. Through the application of the inventive method and the
inventive apparatus, the valuable by-product hydrogen is generated
in addition to the usable product benzene.
[0039] The foregoing disclosure has been set forth merely to
illustrate the invention and is not intended to be limiting. Since
modifications of the disclosed embodiments incorporating the spirit
and substance of the invention may occur to persons skilled in the
art, the invention should be construed to include everything within
the scope of the appended claims and equivalents thereof.
* * * * *