U.S. patent application number 12/278703 was filed with the patent office on 2009-01-29 for fluid catalytic cracking process.
Invention is credited to Jan Lodewijk Maria Dierickx, George A. Hadjigeorge, Colin John Schaverien.
Application Number | 20090026112 12/278703 |
Document ID | / |
Family ID | 40328239 |
Filed Date | 2009-01-29 |
United States Patent
Application |
20090026112 |
Kind Code |
A1 |
Dierickx; Jan Lodewijk Maria ;
et al. |
January 29, 2009 |
FLUID CATALYTIC CRACKING PROCESS
Abstract
A fluid catalytic cracking process for the preparation of
cracked products by contacting in a reactor a hydrocarbon feedstock
with a cracking catalyst, wherein the hydrocarbon feedstock
comprises a paraffinic feedstock and triglycerides.
Inventors: |
Dierickx; Jan Lodewijk Maria;
(Amsterdam, NL) ; Hadjigeorge; George A.; (Sugar
Land, TX) ; Schaverien; Colin John; (Amsterdam,
NL) |
Correspondence
Address: |
SHELL OIL COMPANY
P O BOX 2463
HOUSTON
TX
772522463
US
|
Family ID: |
40328239 |
Appl. No.: |
12/278703 |
Filed: |
February 9, 2006 |
PCT Filed: |
February 9, 2006 |
PCT NO: |
PCT/EP07/51262 |
371 Date: |
August 7, 2008 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
|
60771646 |
Feb 9, 2006 |
|
|
|
Current U.S.
Class: |
208/119 |
Current CPC
Class: |
Y02P 30/20 20151101;
C10G 2300/1022 20130101; C10G 3/57 20130101; C10G 2300/1014
20130101; C10G 11/18 20130101; C10G 3/49 20130101; C10L 1/023
20130101 |
Class at
Publication: |
208/119 |
International
Class: |
C10G 11/05 20060101
C10G011/05 |
Claims
1. A fluid catalytic cracking process for the preparation of
cracked products by contacting in a reactor a hydrocarbon feedstock
with a cracking catalyst, wherein the hydrocarbon feedstock
comprises a paraffinic feedstock and triglycerides.
2. A process according to claim 1, wherein the paraffinic feedstock
comprises at least 50 wt % of paraffins.
3. A process according to claim 1, wherein the weight ratio between
the paraffinic feedstock and the triglycerides present in the
hydrocarbon feedstock is in the range of from 20:1 to 1:5.
4. A process according to claim 1, wherein the hydrocarbon
feedstock comprises up to 90 wt % of a conventional FCC
feedstock.
5. A process according to claim 1, wherein the hydrocarbon
feedstock comprises vegetable oil.
6. A process according to claim 1, wherein the paraffinic feedstock
is a hydrowax.
7. A process according to claim 1, wherein the paraffinic feedstock
is a Fischer-Tropsch derived hydrocarbon stream.
8. A process according to claim 1, wherein the cracking catalyst
comprises a large pore size zeolite.
9. A process according to claim 8, wherein the large pore zeolite
is USY.
10. A process according to claim 1, wherein the cracking catalyst
further comprises a medium pore zeolite.
11. A process according to claim 10, wherein the medium pore size
zeolite is ZSM-5.
12. A process according to claim 1, wherein the paraffinic
feedstock comprises at least 70 wt % of paraffins.
13. A process according to claim 1, wherein the weight ratio
between the paraffinic feedstock and the triglycerides present in
the hydrocarbon feedstock is in the range of from 5:1 to 1:2.
14. A process according to claim 1, wherein the hydrocarbon
feedstock comprises up to 70 wt % of a conventional FCC
feedstock.
15. A process according to claim 1, wherein the hydrocarbon
feedstock comprises palm oil.
16. A process according to claim 1, wherein the hydrocarbon
feedstock comprises rapeseed oil.
17. A process according to claim 2, wherein the weight ratio
between the paraffinic feedstock and the triglycerides present in
the hydrocarbon feedstock is in the range of from 20:1 to 1:5.
18. A process according to claim 2, wherein the hydrocarbon
feedstock comprises up to 90 wt % of a conventional FCC
feedstock.
19. A process according to claim 3, wherein the hydrocarbon
feedstock comprises up to 90 wt % of a conventional FCC
feedstock.
20. A process according to claim 2, wherein the weight ratio
between the paraffinic feedstock and the triglycerides present in
the hydrocarbon feedstock is in the range of from 5:1 to 1:2.
Description
FIELD OF THE INVENTION
[0001] The present invention relates to a fluid catalytic cracking
process.
BACKGROUND OF THE INVENTION
[0002] In fluid catalytic cracking processes a preheated
hydrocarbon feedstock of a high boiling point range is brought into
contact with a hot cracking catalyst in a catalytic cracking
reactor, usually a riser. The feed is cracked into lower boiling
products, such as dry gas, LPG, gasoline, and cycle oils.
Furthermore, coke and non-volatile products deposit on the catalyst
resulting in a spent catalyst. The reactor exits into a separator
wherein the spent catalyst is separated from the reaction products.
In the next step the spent catalyst is stripped with steam to
remove the non-volatile hydrocarbon products from the catalyst. The
stripped catalyst is passed to a regenerator in which coke and
remaining hydrocarbon materials are combusted and wherein the
catalyst is heated to a temperature required for the cracking
reactions. Hereafter the hot regenerated catalyst is returned to
the reactor.
[0003] As hydrocarbon feedstock a feedstock comprising a large
portion of paraffins can be cracked. However, cracking such a
paraffin rich hydrocarbon feedstock, such as for example a
Fischer-Tropsch product, is not straightforward.
[0004] U.S. Pat. No. 4,684,756 describes a process to prepare a
gasoline fraction by fluid catalytic cracking of a Fischer-Tropsch
wax as obtained in an iron catalysed Fischer-Tropsch process. The
gasoline yield is 57.2 wt %. A disadvantage of the process
disclosed in U.S. Pat. No. 4,684,756 is that the yield to gasoline
is relatively low.
[0005] EP-A-454256 describes a process to prepare lower olefins
from a Fischer-Tropsch product by contacting this product with a
ZSM-5 containing catalyst at a temperature of between 580 and
700.degree. C. in a moving bed reactor at a catalysts to oil ratio
of between 65 and 86 kg/kg.
[0006] WO-A-2004/106462 describes a process wherein a relatively
heavy Fischer-Tropsch product and a catalyst system comprising a
catalyst, which catalyst comprises an acidic matrix and a large
pore molecular sieve, are contacted, yielding a gasoline product
having a high content of iso-paraffins and olefins, compounds which
greatly contribute to a high octane number.
[0007] A disadvantage of processing such a paraffinic feed in an
FCC unit is that the coke make is too low. Coke on the catalyst is
removed by oxidation in a so-called FCC regenerator. In such a
process step the catalyst temperature increases due to exothermic
reactions and reaches a temperature that makes it suitable for use
in the actual catalytic cracking step. If the coke content of the
catalyst is too low additional fuel is to be added to the
regenerator and this situation is obviously not desired.
[0008] NL-A-8700587 describes catalytic cracking of water-free
butter to hydrocarbon products, like C.sub.4 gases and lighter
gases, gasoline (C.sub.5-216.degree. C.), light cycle oils and
coke, over a type RE-USY catalyst further comprising an active
crystalline aluminium oxide matrix.
[0009] It is the object of the present invention to achieve a
process which is better heat balanced than the prior art
processes.
SUMMARY OF THE INVENTION
[0010] It has now been found that the above can be achieved by
performing the fluid catalytic cracking of the paraffinic feedstock
in the presence of triglycerides.
[0011] Accordingly, the invention provides a fluid catalytic
cracking process for the preparation of cracked products by
contacting in a reactor a hydrocarbon feedstock with a cracking
catalyst, wherein the hydrocarbon feedstock comprises a paraffinic
feedstock and triglycerides.
[0012] It has been found that by cracking a mixture of a paraffinic
feedstock and triglycerides, more coke is formed on the cracking
catalyst. An additional advantage of cracking the mixture is that a
gasoline is obtained having a higher octane number. Applicant
further found that by choosing the right balance between the
paraffinic feedstock on the one hand and the triglycerides on the
other hand, a gasoline product may be obtained having a sulphur
content of less than 10 ppm, an aromatic content of lower than 35
vol %, preferably lower than 25 vol %, and an octane number of
higher than 87. The triglycerides present in the hydrocarbon
feedstock are cracked and the products formed result in improved
RON octane numbers of the total product.
DETAILED DESCRIPTION OF THE INVENTION
[0013] Triglycerides are glycerides in which the glycerol is
esterified with three fatty acids. Preferably, the triglycerides
that are being used in the process according to the invention
comprise fatty acids wherein the fatty acid moiety ranges from 4 to
30 carbon atoms, the fatty acids most commonly being saturated or
containing 1, 2 or 3 double bonds. Triglycerides are the main
constituent in vegetable oil, fish oil and animal fat.
[0014] Preferably, the hydrocarbon feedstock comprises vegetable
oil, animal fat or fish oil to provide the triglycerides. The
vegetable oil, animal fat or fish oil does not need to be in
anhydrous or pure form or to be subjected to prior hydrogenation.
The oil or fat may contain variable amounts of free fatty acids
and/or esters both of which may also be converted to hydrocarbons
during the process of this invention. The oil or fat may further
comprise carotenoids, hydrocarbons, phosphatides, simple fatty
acids and their esters, terpenes, sterols, fatty alcohols,
tocopherols, polyisoprene, carbohydrates and proteins.
[0015] Suitable vegetable oils include rapeseed oil, palm oil,
coconut oil, corn oil, soya oil, safflower oil, sunflower oil,
linseed oil, olive oil and peanut oil. Suitable animal fats include
pork lard, beef fat, mutton fat and chicken fat. Mixtures of oils
or fats of different origins may be used as feed to the catalytic
conversion step. Thus, mixtures of the vegetable oils, animal fats,
fish oils, and mixtures which include vegetable oil, animal fat
and/or fish oil may be used. Preferred oils are rapeseed oil and
palm oil, in particular palm oil. It has been found that the use of
palm oil results in a higher conversion to cracked products and in
higher yields to gasoline.
[0016] The hydrocarbon feedstock may further comprise natural fatty
acids and esters other than triglycerides, for example fatty acid
methyl esters derived from transesterification of the above plant
oils and animal oils.
[0017] Without wishing to be bound to any theory, we found that
catalytic cracking of triglycerides seems to be a stepwise process
where in the first step fatty acids molecules and the glycerol
backbone are being formed. The fatty acid molecules are
subsequently cracked into lighter components. We found that, in the
presence of a cracking catalyst, the conversion of the
triglycerides into fatty acids is almost instantaneous, while the
next step, being the conversion of fatty acids, depends on factors
such as catalyst to oil ratio, type of catalyst, temperature and
residence time.
[0018] Typically, one expects that the oxygen present in the
triglycerides is being converted to CO.sub.2 in the catalytic
cracking step. We, however, found that most of the oxygen is
converted to water as by-product. This water will already function
as stripping gas and will be separated from the valuable products
in the stripping step of the fluid catalytic cracking process.
[0019] Examples of suitable paraffinic feedstocks are a
Fischer-Tropsch derived hydrocarbon stream or hydrowax.
[0020] Hydrowax is the bottoms fraction of a hydrocracker. With a
hydrocracker in the context of the present invention is meant a
hydrocracking process of which the main products typically are
naphtha, kerosene and gas oil. The conversion, expressed in the
weight percentage of the fraction in the feed to the hydrocracker
boiling above 370.degree. C. to hydrocarbons boiling below
370.degree. C., is typically above 50 wt %. Examples of
hydrocracking processes which may yield a bottoms fraction that can
be used in the present process, are described in EP-A-699225,
EP-A-649896, WO-A-97/18278, EP-A-705321, EP-A-994173 and U.S. Pat.
No. 4,851,109.
[0021] By "Fischer-Tropsch derived hydrocarbon stream" is meant
that the hydrocarbon stream is a product from a Fischer-Tropsch
hydrocarbon synthesis process or derived from such product by a
hydroprocessing step, i.e. hydrocracking, hydro-isomerisation
and/or hydrogenation.
[0022] The Fischer-Tropsch reaction converts carbon monoxide and
hydrogen into longer chain, usually paraffinic, hydrocarbons:
n(CO+2H.sub.2)=(--CH.sub.2--).sub.n+nH.sub.2O+heat,
in the presence of an appropriate catalyst and typically at
elevated temperature, for example 125 to 300.degree. C., preferably
175 to 250.degree. C., and pressure, for example 5 to 100 bar,
preferably 12 to 80 bar. Hydrogen:carbon monoxide ratios other than
2:1 may be employed if desired.
[0023] The carbon monoxide and hydrogen is typically derived from a
hydrocarbonaceous feedstock by partial oxidation. Suitable
hydrocarbonaceous feedstocks include gaseous hydrocarbons such as
natural gas or methane, coal, biomass, or residual fractions from
crude oil distillation.
[0024] The Fischer-Tropsch derived hydrocarbon stream may suitably
be a so-called syncrude as described in for example GB-A-2386607,
GB-A-2371807 or EP-A-0321305. Other suitable Fischer-Tropsch
hydrocarbon streams may be hydrocarbon fractions boiling in the
naphtha, kerosene, gas oil, or wax range, as obtained from the
Fischer-Tropsch hydrocarbon synthesis process, optionally followed
by a hydroprocessing step.
[0025] Preferably, the Fischer-Tropsch hydrocarbon stream product
has been obtained by hydroisomerisation of hydrocarbons directly
obtained in the Fischer-Tropsch hydrocarbon synthesis reaction. The
use of a hydro-isomerised hydrocarbon fraction is advantageous
because it contributes to a high yield in gasoline due to the high
content of iso-paraffins in said fraction. A hydro-isomerised
fraction boiling in the kerosene or gas oil range may suitable be
used as the Fischer-Tropsch derived hydrocarbon stream. Preferably,
however, a higher boiling hydro-isomerised fraction is used as
feed.
[0026] A particularly suitable hydro-isomerised hydrocarbon
fraction is a fraction which has a T10 wt % boiling point of
between 350 and 450.degree. C. and a T90 wt % of between 450 and
600.degree. C. and a wax content of between 5 and 60 wt %. Such
fraction is typically referred to as waxy raffinate. Preferably,
the wax content is between 5 and 30 wt %. The wax content is
measured by solvent dewaxing at -27.degree. C. in a 50/50 vol/vol
mixture of methyl ethyl ketone and toluene. Examples of such a
hydrocarbon streams are the commercially available Waxy Raffinate
product as is marketed by Shell MDS (Malaysia) Sdn Bhd snf the waxy
raffinate product as obtained by the process described in
WO-A-02/070630 or in EP-B-0668342.
[0027] The paraffinic feedstock comprises preferably at least 50 wt
% paraffins, more preferably at least 70 wt % paraffins. With
paraffins both normal and iso-paraffins are meant. The paraffin
content of the paraffinic feedstocks in the context of the present
invention are measured by means of comprehensive multi-dimensional
gas chromatography (GC.times.GC), as described in P. J.
Schoenmakers, J. L. M. M. Oomen, J. Blomberg, W. Genuit, G. van
Velzen, J. Chromatogr. A, 892 (2000) p. 29 and further.
[0028] The hydrocarbon feedstock according to the present invention
comprises both a paraffinic feedstock and triglycerides.
Preferably, the weight ratio between the amount of paraffinic
feedstock and the amount of triglycerides present in the
hydrocarbon feedstock is between 20:1 to 1:5, more preferably
between 5:1 to 1:2.
[0029] The hydrocarbon feedstock may optionally also comprise a
component not being a triglyceride or a paraffinic feedstock.
Suitable components are so-called conventional FCC feedstocks,
which are typically derived from crude oil refining and which are
less paraffinic than the above described paraffinic feeds. The
conventional FCC feedstock that can be used in the process
according to the invention includes high boiling non-residual crude
oil fractions, such as vacuum gas oil, straight run (atmospheric)
gas oil, coker gas oils and residues from atmospheric or vacuum
distillation of crude oil. These feedstocks have boiling points
preferably ranging from 220.degree. C. to 650.degree. C., more
preferably ranging from 300.degree. C. to 600.degree. C.
[0030] The quantity of the conventional FCC feedstock relative to
the paraffinic feedstock and triglycerides may vary depending on
feedstock availability and on the quality of the desired product.
In the process according to the invention the hydrocarbon feedstock
may comprise up to 90 wt % of the conventional FCC feedstock,
preferably up to 70 wt % of the conventional FCC feedstock, more
preferably up to 50 wt % of the conventional FCC feedstock, even
more preferably up to 40 wt % of the conventional FCC feedstock. An
advantage of processing a mixture of conventional FCC feedstock,
paraffinic feedstock and triglycerides is for example that gasoline
with a reduced aromatic content is produced. Another advantage is
that when triglycerides and a paraffinic feedstock are added to a
heavy conventional FCC feedstock, an increased yield of lower
olefins is obtained. The advantages of the present invention become
more pronounced at lower content of the conventional FCC feedstock
in the feed.
[0031] Thus, by choosing the right balance between the paraffinic
feedstock and triglycerides on the one hand and the conventional
FCC feedstock on the other hand a gasoline product may be obtained
having the desired properties such as an acceptable octane number,
a low sulphur content and a desired aromatic content. The
properties of the cracked products can be adjusted.
[0032] In the process according to the invention, the cracking
catalyst comprises a large pore zeolite. With a large pore zeolite,
a zeolite is meant comprising a porous, crystalline aluminosilicate
structure having a porous internal cell structure on which the
major axis of the pores are in the range from 0.62 to 0.8
nanometer. Axis of zeolites are depicted in the `Atlas of Zeolite
Structure Types`, of W. M. Meier, D. H. Olson, and Ch. Baerlocher,
Fourth Revised Edition 1996, Elsevier, ISBN 0-444-10015-6. Examples
of such large pore zeolites are FAU or faujasite, preferably
synthetic faujasite, like zeolite Y, USY, Rare Earth Y (=REY) or
Rare Earth USY (REUSY). According to the present invention
preferably USY is used as the large pore zeolite.
[0033] The cracking catalyst preferably further comprises a medium
pore zeolite if a high yield of propylene is desired. By a medium
pore zeolite that can be used in the present invention is
understood a zeolite comprising a porous, crystalline
aluminosilicate structure having a porous internal cell structure
on which the major axis of the pores are in the range from 0.45 to
0.62 nanometer. Examples of such medium pore zeolites are of the
MFI structural type such as ZSM-5, the MTW type, such as ZSM-12,
the TON structural type such as theta one, and the FER structural
type such is ferrierite. According to the present invention
preferably ZSM-5 is used as the medium pore zeolite.
[0034] The weight ratio of large pore zeolite to medium pore size
zeolite in the cracking catalyst is preferably in the range from
99:1 to 70:30, more preferably in the range from 98:2 to 85:15.
[0035] The total amount of large pore size zeolite and/or medium
pore zeolite that is present in the cracking catalysts is
preferably in the range from 5 to 40 wt %, more preferably in the
range from 10 to 30 wt %, even more preferably in the range from 10
to 25 wt % relative to the total mass of the catalyst.
[0036] Next to the large or medium pore size zeolite, the catalysts
may comprise one or more porous, inorganic refractory metal oxide
binder materials or supports and/or active matrix materials. These
binder materials or supports may or may not contribute to the
cracking reaction. Examples of such binder materials are silica,
alumina, titania, zirconia and magnesium oxide, or combinations of
two or more of them. Also organic binders may be used.
[0037] The temperature at which the hydrocarbon feedstock and the
cracking catalyst are contacted is preferably between 450 and
650.degree. C. More preferably, the temperature is above
475.degree. C., even more preferably above 500.degree. C. Good
gasoline yields are seen at temperatures above 600.degree. C.
However, temperatures above 600.degree. C. will also give rise to
thermal cracking reactions and the formation of non-desirable
gaseous products like methane and ethane. For this reason the
temperature is preferably below 600.degree. C.
[0038] The process may be performed in various types of reactors.
In order to simplify catalyst regeneration, preference is given to
either a fast fluidised bed reactor or a riser reactor. If the
process is performed in a riser reactor the preferred contact time
is between 1 and 10 seconds and more preferred between 2 and 7
seconds. The catalyst to oil (hydrocarbon feedstock) ratio is
preferably between 2 and 20 kg/kg. It has been found that good
results may be obtained at a catalyst to oil ratio above 6 kg/kg,
since a higher catalyst to oil ratio results in a higher amount of
coke on the catalyst.
EXAMPLES
[0039] The invention is further illustrated by the following
Examples. The most important properties of hydrowax are shown in
table 1.
TABLE-US-00001 TABLE 1 Feed properties Hydrowax Density (D70/4)
0.807 Nitrogen coul (ppmw) 2 Viscosity (100.degree. C.) (cSt) 6.73
Sulphur (wt %) 0.5 Total aromatics (wt %) 6.07 Carbon (wt %) 85.7
Hydrogen (wt %) 14.3 Initial Boiling Point (.degree. C.) 196 Final
Boiling Point (.degree. C.) 608
Example 1
[0040] Catalytic cracking experiments were carried out in a
micro-riser reactor that operates in an isothermal plug-flow
regime. The micro-riser reactor is a once-through bench-scale fluid
catalytic cracking reactor that simulates the hydrodynamics of an
industrial FCC reactor. The reactor temperature was set to
525.degree. C. The length of the reactor was in these experiments
21.2 meters. The catalyst used was a commercial silica sol based
FCC equilibrium catalyst (e-cat), containing 11 wt % USY zeolite
crystals. Before each experiment, the catalyst was regenerated in a
fluidised bed reactor, where coke was combusted in air at
600.degree. C. for three hours. The catalyst was fed to the reactor
by means of a catalyst feeder. Nitrogen was used to facilitate the
catalyst flow. The oil feed was fed through a pulse-free syringe
pump to the pre-heated oven where it was partially evaporated. In
the last part before the injection point the oil was completely
evaporated and adopted the reaction temperature, as well as the
catalyst. The feed was injected perpendicularly into the catalyst
stream. The feed consisted of pure hydrowax, or hydrowax blended
with 20 wt % or 40 wt % of crude degummed rapeseed oil.
[0041] Sample collection started when the system had reached
steady-state operation. Separation of the catalyst and gaseous
product took place by means of a cyclone. During the steady-state
operation the catalyst was stored under reaction conditions and was
afterwards stripped with nitrogen. The effluent gas was led through
three condensers in series operating at 25, -60, and -60.degree.
C., respectively. Any uncondensed products were captured in a gas
bag. The C.sub.1-C.sub.4 hydrocarbon components in the gas bag were
determined by means of gas chromatography. The entrained C.sub.5
and C.sub.6 hydrocarbons were detected as two separate lumps by
this analysis method and added to the gasoline fraction. The liquid
product was analysed by simulated distillation. This gave the
amounts of product in terms of lumps of boiling ranges: gasoline
(C.sub.5-215.degree. C.), Light Cycle Oil (LCO, 215-325.degree.
C.), and Heavy Cycle Oil and Slurry Oil (HCO+SO, 325+.degree. C.).
The coke on the catalyst was determined with a LECO C-400 carbon
analyser. The results are presented in table 2.
[0042] In comparison with 100% hydrowax, addition of rapeseed oil
(RSO) results in increasing amounts of coke and LCO. Furthermore, a
clear increase in the calculated RON is observed for the
catalytically cracked blend of hydrowax with 40 wt % rapeseed oil
as compared to 100% hydrowax.
TABLE-US-00002 TABLE 2 HWX + HWX + 100% 20 wt % 40 wt % Experiment
HWX RSO RSO CTO (g cat/g oil) 3.8 4.5 4.6 Contact time (s) 4.4 4.4
4.5 Yields (wt %) Coke 2.0 2.1 3.3 Gas 11.7 9.2 7.9 Gasoline (C5 -
215.degree. C.) 60.2 59.4 55.7 LCO (215-325.degree. C.) 15.7 18.1
20.7 HCO + SO (325+) 11 12 RON 85.7 89.2
Example 2
[0043] In a small-scale fluidised bed reactor the catalytic
cracking blends of hydrowax, with rapeseed oil and palm oil (at 5,
10, 25 wt %) using a equilibrium catalysts, e-cat2, was performed.
The experiments were done in a reactor in which 10 grams of the
commercial e-catalyst was constantly fluidised with nitrogen.
Dependent on the cat/oil ratio an amount of 1.25 to 3.33 grams of
oil was injected in the reactor. During stripping the liquid
products were collected in glass vessels (receivers) in a bath at a
temperature of -15.degree. C. The gas produced was analysed online
with a gas chromatograph. After stripping for 660 seconds, the
amount of coke formed on the catalyst was determined by burning the
coke from the catalyst in a regeneration step. During 40 minutes
the temperature of the reactor was at 650.degree. C. in an air
environment. The coke was converted to CO.sub.2 and measured
online. After regeneration the reactor was cooled to the reaction
temperature and a new injection was started. The results are
presented in tables 3 and 4.
TABLE-US-00003 TABLE 3 Product distribution using e-cat2 at
500.degree. C. (at Cat/Oil ratio 6.3) of hydrowax (HWX) and
mixtures of hydrowax and rapeseed oil (RSO). 100% HWX with HWX with
HWX with HWX 5% RSO 10% RSO 25% RSO CTO (g cat/g oil) 6.3 6.3 6.3
6.3 Conversion 87.1 87.9 86.5 82.4 CO 0.0 0.0 0.0 0.1 CO.sub.2 0.0
0.1 0.1 0.2 H.sub.2O n/a 0.6 1.2 2.8 Coke 2.0 2.2 2.5 3.1 Drygas
1.0 1.0 1.1 1.2 LPG 24.2 25.2 24.7 21.6 Gasoline 59.9 59.5 58.2
56.5 (C5 - 215.degree. C.) LCO 7.3 7.3 8.0 10.0 (215-325.degree.
C.) HCO + SO (325+) 5.6 4.2 4.2 4.5 GC-RON 86.3 86.7 87.3 87.7
GC-MON 77.4 77.8 78.4 78.5
TABLE-US-00004 TABLE 4 Product distribution using e-cat2 at
500.degree. C. (at Cat/Oil ratio 6) of hydrowax (HWX) and mixtures
of hydrowax and palm oil. HWX + 5% HWX + 10% HWX + 25% palm oil
palm oil palm oil CTO (g cat/g oil) 5.8 5.7 5.5 Conversion 88.2
89.9 83.7 CO 0.1 0.1 0.3 CO.sub.2 0.1 0.1 0.3 H.sub.2O 0.6 1.1 2.7
Coke 1.8 2.0 2.4 Drygas 0.9 1.0 1.0 LPG 23.6 23.4 21.3 Gasoline (C5
- 215.degree. C.) 61.8 63.5 58.9 LCO (215-325.degree. C.) 7.5 6.3
8.4 HCO + SO (325+) 3.7 2.5 4.6 GC-RON 88.0 87.8 88.3 GC-MON 79.4
79.4 79.7
* * * * *