CA2009986A1 - Process for the conversion of a hydrocarbonaceous feedstock - Google Patents
Process for the conversion of a hydrocarbonaceous feedstockInfo
- Publication number
- CA2009986A1 CA2009986A1 CA002009986A CA2009986A CA2009986A1 CA 2009986 A1 CA2009986 A1 CA 2009986A1 CA 002009986 A CA002009986 A CA 002009986A CA 2009986 A CA2009986 A CA 2009986A CA 2009986 A1 CA2009986 A1 CA 2009986A1
- Authority
- CA
- Canada
- Prior art keywords
- feedstock
- process according
- catalyst
- zeolite
- conversion
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
- C10G35/10—Catalytic reforming with moving catalysts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/16—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "moving bed" method
Abstract
A B S T R A C T
PROCESS FOR THE CONVERSION OF A
HYDROCARBONACEOUS FEEDSTOCK
A process for the conversion of a straight-run hydrocarbonaceous feedstock, such as a gas oil, comprises contacting the feedstock with a moving bed of a zeolitic catalyst which comprises a zeolite with a pore diameter of 0.3 to 0.7 nm at a temperature above 480 °C for less than 10 seconds.
PROCESS FOR THE CONVERSION OF A
HYDROCARBONACEOUS FEEDSTOCK
A process for the conversion of a straight-run hydrocarbonaceous feedstock, such as a gas oil, comprises contacting the feedstock with a moving bed of a zeolitic catalyst which comprises a zeolite with a pore diameter of 0.3 to 0.7 nm at a temperature above 480 °C for less than 10 seconds.
Description
Z~ 136 , PROCESS FOR THE CONVERSION OF A
HYDROCARBONACEOUS FEEDSTOCK
The present invention relates to a process for the conversion of a hydrocarbonaceous feedstock.
US 4,171,257 describes a process for upgrading a hydrocarbonaceous feedstock by contacting the feedstock with a ZSM-5 crystalline aluminosilicate catalyst at a pressure below 14 bar, a temperature of 260 to 427 C
and a space velocity of 0.1 to 15 l/l.h. The feedstock, exemplified as gas oil having a boiling point range of 230 to 437 C, must contain less than 5 ppmw of nitrogen containing compounds, calculated as nitrogen.
The upgraded product includes olefinic hydrocarbons, such as propene and butenes.
The production of olefins is desirable as their reactivity renders them suitable for conversion to further products, in contrast to the low value lower paraffins. However, the above described process has the drawback that the initial feedstock must have been severely denitrified in order to avoid rapid catalyst deactivationO
It is also known from EP-B-131986 and US 3,758,403 to employ mixtures of aluminosilicate catalysts comprising a large pore ~diameter crystalline aluminium silicate and a narrow pore silicate such as ZSM-5 in the production of gasoline. C3 and C4 olefin byproduct obtained can be alkylated to increase the overall gasoline yield. The space velocities and other conditions employed in the examples given indicate the use of fixed bed reactors with comparatively high catalyst contact times.
.
.
Z~99~
It has surprisingly been found that a comparatively high yield of olefins can be obtain2d, under less stringent conditions as regards nitrogen content, using certain æeolitic catalysts, at high temperature with a short contact time of the feedstock with the catalyst. Furthermore, it has bPen surprisingly found that the conversion is suitable for comparatively heavy straight run hydrocarbon feedstocks and a product rich in lower 012fins can be obtained therefrom.
Accordingly, the present invention provides a process for the conversion of a straight-run hydro-carbonaceous feedstock containing hydrocarbons having such a boiling range that an amount thereof boils at a temperature of at least 330 ~C, which process comprises contacting the feedstock with a moving bed of a zeolitic catalyst comprising a zeolite with a pore diameter of 0.3 to 0.7 nm, preferably 0.5 to 0.7 nm, at a temperature of greater than 480 C during less than 10 seconds.
The feedstock is contacted with the zeolitic catalyst for less than 10 seconds. Suitably, the minimum contact time is 0.1 second. Very good results are obtainable with a process in which the feedstock is contacted with the zeolitic catalyst during 0.2 to 6 seconds.
The temperature du~ing the reaction is relatively high. It is this combination of high temperature and short contact time which allows a high conversion to 30 olefins. A preferred temperature range is 500 to 900 C, more preferably 550 to 850 C.
The zeolitic catalyst may comprise one or more zeolites with a pore diameter of from 0.3 to 0.7 nm.
The catalyst suitably further comprises a refractory oxide that serves as binder material. Suitable Z(~9~
~ 3 refractory oxides include alumina, silica, silica-alumina, magnesia, titania, zirconia and mixtures thereof. Alumina is especially preferred. The weight ratio of refractory oxide and zeolite suitably ranges from 10:90 to 90:10, preferably from 50:50 to 85:15. The catalyst may comprise up to about 40% by weight of further zeolites with a pore diameter above 0.7 nm. Suitable examples of such zeolites include the ~aujasite-type zeolites, zeolite beta, zeolite omega and in particular zeolite X and Y. The zeolitic catalyst preferably comprises as zeolite substantially only zeolites with a pore diame~er of from 0.3 to 0.7 nm.
The term zeolite in this specification is not to be regarded as comprising only crystalline aluminium silicates~ The term also includes crystalline silica (silicalite), silicoaluminophosphates (SAPO), chromosilicates, gallium silicates, iron silicates, aluminium phosphates (ALPO), titanium aluminosilicates (TASO~, boron silicates, titanium aluminophosphates (TAPO) and iron aluminosilicates.
Examples of zeolites that may be used in the process of the invention and that have a pore diameter of 0.3 to 0.7 nm, include SAPO-4 and SAP0-11, which are 25 described in US-A-4,440,871, ALP0-11, described in US-A-4,310,440, TAPO-ll, described in US-A-4,500,651, TASO-45, described in EP~-A-229,295, boron silicates, described in e.g. US-A~4,254,297, aluminium silicates like erionite, ferrierite, theta and the ZSM-type 30 zeolites such as ZSM-5, ZSM-ll, ZSM-12, Z5M-35, ZSM-23, and ZSM-38. Preferably the zeolite is selected from the group consisting of crystalline metal silicates having a ZSM~5 structure, ferrierite, erionite and mixtures thereof~ Suitable examples of crystalline metal silicates with ZSM-5 structure are aluminium, gallium, 20~
~, iron, scandium, rhodium and/or scandium silicates as described in e.g. Gs-B-2,llO,559.
During the preparation of the zeolites usually a significant amount of alkali metal oxide is present in the prepared zeolite. Preferably the amount of alkali metal is removed by methods known in the art, such as ion exchange, optionally followed by calcination, to yield the zeolite in its hydrogen form. Preferably the zeolite used in the present process is substantially in its hydrogen form.
The pressure in the present process can be varied within wide ranges. It is, however, preferred that the pressure is such that at the prevailing temperature the feedstock is substantially in its gaseous phase or brought thereinto by contact with the catalyst. Then it is easier to achieve the short contact times envisaged.
Hence, the pressure is preferably relatively low. This can be advantageous since no expensive compressors and high-pressure vessels and other equipment are necessary. A suitable pressure range is from l to l0 bar. Subatmospheric pressures are possible, but not preferred. It can be economically advantageous to operate at atmospheric pressure. Other gaseous materials may be present during the conversion such as steam and/or nitrogen.
The present process is carried out in a moving bed. The bed of catalyst may move upwards or downwards.
When the bed moves upwards a procsss somewhat similar to a fluidized;catalytic cracking process is obtained.
During the process some coke forms on the catalyst. Therefore, it is advantageous to regenerate the catalyst. Preferably the catalyst is regenerated by subjecting it, after having been contacted with the ~eedstock~ to a treatment with an oxidizing gas, such as air. A continuous regeneration, similar ko the ;~0~ 6 regeneration carried out in a fluidized catalytic cracking process, is especially preferred.
If the coke formation does not occur at too high a rate, it would be possible to arrange for a process in which the residence time of the catalyst particles in a reaction zone is longer than the residence time of the feedstock in ~he reaction zoneO Of course the contact time between feedstock and catalyst should be less than 10 seconds. The contact time generally corresponds with the residence time of the feedstock. Suitably the residence time of the catalyst is from 1 to 20 times the residence time o~ the feedstock.
The catalyst/feedstock weight ratio may vary widely, for example up to 150 kg of catalyst per kg of feedstock or even more. Preferably, the catalyst/feedstock weight ratio is from 20 to 100:1.
The feedstock which is to be converted in the present process comprises hydrocarbons which have a boiling point of at least 330 C. By means of this feature relatively light petroleum fractions, such as naphtha and kerosine, have been excluded. Preferably the feedstock has such a boiling range that at least 50% by weight thereof boils at a temperature of 330 C.
Suitable feedstocks include vacuum distillates, long residues, deasphalted residual oils, paraffinic feedstocks and atmospheric distillates which fulfil the requirement as to boiling range, such as gas oils.
Preferably, the feedstock is a gas oil or vacuum gas oil. Nhen these feedstocks are subjected to the present process a gas oil with a very low pour point and an olefin-rich gaseous fraction are obtained.
One of the advantages of the present invention over the process according to US 4,171,257 resides in the fact that a feedstock with a nitrogen content greater than 5 ppmw may be used with substantially no 9~6 effect on the catalyst activity. Suitable feedstocks may have a nitrogen content of more than lO ppmw, calculated as nitrogen. The feedstock may even have a nitrogen content of looo ppmw or more, calculated as nitrogen.
The invention will now be further described with reference to the following example.
EXAMPLE
The feedstock in this example was a gas oil having the following properties:
IBP, C 213 20 %wt 331 50 %wt 379 90 %wt 421 pour point, C19.5 flash point, C147 carbon, %wt 86.6 hydrogen, %wt13.1 sulphur, %wt 0.3 nitrogen, ppmw330 The gas oil was treated in a down ~low reactor in which co-currently a fl~w of feedstock and catalyst particles, having an average particle size of 74 micrometers, was passed downwards. The catalyst used comprised ZSM-5, in hydrogen ~orm, in an alumina matrix (weight ratio ZSM-5/alumina was 1:3). All experiments were carried out at atmospheric pressure. Further process conditions and the results of the experiments are indicated in the table below.
HYDROCARBONACEOUS FEEDSTOCK
The present invention relates to a process for the conversion of a hydrocarbonaceous feedstock.
US 4,171,257 describes a process for upgrading a hydrocarbonaceous feedstock by contacting the feedstock with a ZSM-5 crystalline aluminosilicate catalyst at a pressure below 14 bar, a temperature of 260 to 427 C
and a space velocity of 0.1 to 15 l/l.h. The feedstock, exemplified as gas oil having a boiling point range of 230 to 437 C, must contain less than 5 ppmw of nitrogen containing compounds, calculated as nitrogen.
The upgraded product includes olefinic hydrocarbons, such as propene and butenes.
The production of olefins is desirable as their reactivity renders them suitable for conversion to further products, in contrast to the low value lower paraffins. However, the above described process has the drawback that the initial feedstock must have been severely denitrified in order to avoid rapid catalyst deactivationO
It is also known from EP-B-131986 and US 3,758,403 to employ mixtures of aluminosilicate catalysts comprising a large pore ~diameter crystalline aluminium silicate and a narrow pore silicate such as ZSM-5 in the production of gasoline. C3 and C4 olefin byproduct obtained can be alkylated to increase the overall gasoline yield. The space velocities and other conditions employed in the examples given indicate the use of fixed bed reactors with comparatively high catalyst contact times.
.
.
Z~99~
It has surprisingly been found that a comparatively high yield of olefins can be obtain2d, under less stringent conditions as regards nitrogen content, using certain æeolitic catalysts, at high temperature with a short contact time of the feedstock with the catalyst. Furthermore, it has bPen surprisingly found that the conversion is suitable for comparatively heavy straight run hydrocarbon feedstocks and a product rich in lower 012fins can be obtained therefrom.
Accordingly, the present invention provides a process for the conversion of a straight-run hydro-carbonaceous feedstock containing hydrocarbons having such a boiling range that an amount thereof boils at a temperature of at least 330 ~C, which process comprises contacting the feedstock with a moving bed of a zeolitic catalyst comprising a zeolite with a pore diameter of 0.3 to 0.7 nm, preferably 0.5 to 0.7 nm, at a temperature of greater than 480 C during less than 10 seconds.
The feedstock is contacted with the zeolitic catalyst for less than 10 seconds. Suitably, the minimum contact time is 0.1 second. Very good results are obtainable with a process in which the feedstock is contacted with the zeolitic catalyst during 0.2 to 6 seconds.
The temperature du~ing the reaction is relatively high. It is this combination of high temperature and short contact time which allows a high conversion to 30 olefins. A preferred temperature range is 500 to 900 C, more preferably 550 to 850 C.
The zeolitic catalyst may comprise one or more zeolites with a pore diameter of from 0.3 to 0.7 nm.
The catalyst suitably further comprises a refractory oxide that serves as binder material. Suitable Z(~9~
~ 3 refractory oxides include alumina, silica, silica-alumina, magnesia, titania, zirconia and mixtures thereof. Alumina is especially preferred. The weight ratio of refractory oxide and zeolite suitably ranges from 10:90 to 90:10, preferably from 50:50 to 85:15. The catalyst may comprise up to about 40% by weight of further zeolites with a pore diameter above 0.7 nm. Suitable examples of such zeolites include the ~aujasite-type zeolites, zeolite beta, zeolite omega and in particular zeolite X and Y. The zeolitic catalyst preferably comprises as zeolite substantially only zeolites with a pore diame~er of from 0.3 to 0.7 nm.
The term zeolite in this specification is not to be regarded as comprising only crystalline aluminium silicates~ The term also includes crystalline silica (silicalite), silicoaluminophosphates (SAPO), chromosilicates, gallium silicates, iron silicates, aluminium phosphates (ALPO), titanium aluminosilicates (TASO~, boron silicates, titanium aluminophosphates (TAPO) and iron aluminosilicates.
Examples of zeolites that may be used in the process of the invention and that have a pore diameter of 0.3 to 0.7 nm, include SAPO-4 and SAP0-11, which are 25 described in US-A-4,440,871, ALP0-11, described in US-A-4,310,440, TAPO-ll, described in US-A-4,500,651, TASO-45, described in EP~-A-229,295, boron silicates, described in e.g. US-A~4,254,297, aluminium silicates like erionite, ferrierite, theta and the ZSM-type 30 zeolites such as ZSM-5, ZSM-ll, ZSM-12, Z5M-35, ZSM-23, and ZSM-38. Preferably the zeolite is selected from the group consisting of crystalline metal silicates having a ZSM~5 structure, ferrierite, erionite and mixtures thereof~ Suitable examples of crystalline metal silicates with ZSM-5 structure are aluminium, gallium, 20~
~, iron, scandium, rhodium and/or scandium silicates as described in e.g. Gs-B-2,llO,559.
During the preparation of the zeolites usually a significant amount of alkali metal oxide is present in the prepared zeolite. Preferably the amount of alkali metal is removed by methods known in the art, such as ion exchange, optionally followed by calcination, to yield the zeolite in its hydrogen form. Preferably the zeolite used in the present process is substantially in its hydrogen form.
The pressure in the present process can be varied within wide ranges. It is, however, preferred that the pressure is such that at the prevailing temperature the feedstock is substantially in its gaseous phase or brought thereinto by contact with the catalyst. Then it is easier to achieve the short contact times envisaged.
Hence, the pressure is preferably relatively low. This can be advantageous since no expensive compressors and high-pressure vessels and other equipment are necessary. A suitable pressure range is from l to l0 bar. Subatmospheric pressures are possible, but not preferred. It can be economically advantageous to operate at atmospheric pressure. Other gaseous materials may be present during the conversion such as steam and/or nitrogen.
The present process is carried out in a moving bed. The bed of catalyst may move upwards or downwards.
When the bed moves upwards a procsss somewhat similar to a fluidized;catalytic cracking process is obtained.
During the process some coke forms on the catalyst. Therefore, it is advantageous to regenerate the catalyst. Preferably the catalyst is regenerated by subjecting it, after having been contacted with the ~eedstock~ to a treatment with an oxidizing gas, such as air. A continuous regeneration, similar ko the ;~0~ 6 regeneration carried out in a fluidized catalytic cracking process, is especially preferred.
If the coke formation does not occur at too high a rate, it would be possible to arrange for a process in which the residence time of the catalyst particles in a reaction zone is longer than the residence time of the feedstock in ~he reaction zoneO Of course the contact time between feedstock and catalyst should be less than 10 seconds. The contact time generally corresponds with the residence time of the feedstock. Suitably the residence time of the catalyst is from 1 to 20 times the residence time o~ the feedstock.
The catalyst/feedstock weight ratio may vary widely, for example up to 150 kg of catalyst per kg of feedstock or even more. Preferably, the catalyst/feedstock weight ratio is from 20 to 100:1.
The feedstock which is to be converted in the present process comprises hydrocarbons which have a boiling point of at least 330 C. By means of this feature relatively light petroleum fractions, such as naphtha and kerosine, have been excluded. Preferably the feedstock has such a boiling range that at least 50% by weight thereof boils at a temperature of 330 C.
Suitable feedstocks include vacuum distillates, long residues, deasphalted residual oils, paraffinic feedstocks and atmospheric distillates which fulfil the requirement as to boiling range, such as gas oils.
Preferably, the feedstock is a gas oil or vacuum gas oil. Nhen these feedstocks are subjected to the present process a gas oil with a very low pour point and an olefin-rich gaseous fraction are obtained.
One of the advantages of the present invention over the process according to US 4,171,257 resides in the fact that a feedstock with a nitrogen content greater than 5 ppmw may be used with substantially no 9~6 effect on the catalyst activity. Suitable feedstocks may have a nitrogen content of more than lO ppmw, calculated as nitrogen. The feedstock may even have a nitrogen content of looo ppmw or more, calculated as nitrogen.
The invention will now be further described with reference to the following example.
EXAMPLE
The feedstock in this example was a gas oil having the following properties:
IBP, C 213 20 %wt 331 50 %wt 379 90 %wt 421 pour point, C19.5 flash point, C147 carbon, %wt 86.6 hydrogen, %wt13.1 sulphur, %wt 0.3 nitrogen, ppmw330 The gas oil was treated in a down ~low reactor in which co-currently a fl~w of feedstock and catalyst particles, having an average particle size of 74 micrometers, was passed downwards. The catalyst used comprised ZSM-5, in hydrogen ~orm, in an alumina matrix (weight ratio ZSM-5/alumina was 1:3). All experiments were carried out at atmospheric pressure. Further process conditions and the results of the experiments are indicated in the table below.
2~
Process conditions:
~eactor temperature, DC 576 Catalyst/oil ratio, g/g 124 Contact time, s 1.8 Product, %w on feed 1 . 9 C
2= 1.4 2 11.3 C3 3.8 cc3= 25.4 4 3.3 c4- 12.2 C5-221 C 15.3 221-37~ C 12.59 370+ C 1.1 Coke 11.1 From the above results it will be seen that a high proportion of the gaseous products was olefinically unsaturated.
Process conditions:
~eactor temperature, DC 576 Catalyst/oil ratio, g/g 124 Contact time, s 1.8 Product, %w on feed 1 . 9 C
2= 1.4 2 11.3 C3 3.8 cc3= 25.4 4 3.3 c4- 12.2 C5-221 C 15.3 221-37~ C 12.59 370+ C 1.1 Coke 11.1 From the above results it will be seen that a high proportion of the gaseous products was olefinically unsaturated.
Claims (10)
1. A process for the conversion of a straight-run hydrocarbonaceous feedstock containing hydrocarbons having such a boiling range that an amount thereof boils at a temperature of at least 330 °C, which process comprises contacting the feedstock with a moving bed of a zeolitic catalyst comprising a zeolite with a pore diameter of 0.3 to 0.7 nm at a temperature of greater than 480 °C during less than 10 seconds.
2. A process according to claim 1 wherein the feedstock is contacted with the zeolitic catalyst during 0.2 to 6 seconds.
3. A process according to claim 1 or 2 wherein the temperature is 550 to 850 °C.
4. A process according to any one of the preceding claims wherein the zeolite has a pore diameter of 0.5 to 0.7 nm.
5. A process according to any one of the preceding claims wherein the zeolite is selected from crystalline metal silicates having a ZSM-5 structure, ferrierite, erionite and mixtures thereof.
6. A process according to any one of the preceding claims in which the zeolite is substantially in its hydrogen form.
7. A process according to any one of the preceding claims wherein the pressure is from 1 to 10 bar.
8. A process according to any one of the preceding claims in which the catalyst/feedstock weight ratio is from 20 to 100:1.
9. A process according to any one of the preceding claims wherein the feedstock is a gas oil.
10. A hydrocarbonaceous product, or a fraction thereof, when obtained by the process of any one of the preceding claims.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8904408.5 | 1989-02-27 | ||
| GB898904408A GB8904408D0 (en) | 1989-02-27 | 1989-02-27 | Process for the conversion of a hydrocarbonaceous feedstock |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2009986A1 true CA2009986A1 (en) | 1990-08-27 |
Family
ID=10652368
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002009986A Abandoned CA2009986A1 (en) | 1989-02-27 | 1990-02-14 | Process for the conversion of a hydrocarbonaceous feedstock |
Country Status (11)
| Country | Link |
|---|---|
| EP (1) | EP0385538B1 (en) |
| JP (1) | JPH02276888A (en) |
| KR (1) | KR910015689A (en) |
| CN (1) | CN1019981C (en) |
| AU (1) | AU628929B2 (en) |
| BR (1) | BR9000880A (en) |
| CA (1) | CA2009986A1 (en) |
| DE (1) | DE69009234T2 (en) |
| ES (1) | ES2056362T3 (en) |
| GB (1) | GB8904408D0 (en) |
| RU (1) | RU2017791C1 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB9026775D0 (en) * | 1990-12-10 | 1991-01-30 | Shell Int Research | Process for the preparation of an olefins-containing mixture of hydrocarbons |
| GB9114390D0 (en) * | 1991-07-03 | 1991-08-21 | Shell Int Research | Hydrocarbon conversion process and catalyst composition |
| US6222087B1 (en) | 1999-07-12 | 2001-04-24 | Mobil Oil Corporation | Catalytic production of light olefins rich in propylene |
| US6835863B2 (en) | 1999-07-12 | 2004-12-28 | Exxonmobil Oil Corporation | Catalytic production of light olefins from naphtha feed |
| EP1195424A1 (en) | 2000-10-05 | 2002-04-10 | ATOFINA Research | A process for cracking an olefin-rich hydrocarbon feedstock |
| DE102012006992A1 (en) * | 2012-04-05 | 2013-10-10 | Linde Aktiengesellschaft | Process for the separation of olefins with mild cleavage |
| WO2017109639A1 (en) | 2015-12-21 | 2017-06-29 | Sabic Global Technologies B.V. | Methods and systems for producing olefins and aromatics from coker naphtha |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3856659A (en) * | 1972-12-19 | 1974-12-24 | Mobil Oil Corp | Multiple reactor fcc system relying upon a dual cracking catalyst composition |
| US4514285A (en) * | 1983-03-23 | 1985-04-30 | Texaco Inc. | Catalytic cracking system |
| US4985136A (en) * | 1987-11-05 | 1991-01-15 | Bartholic David B | Ultra-short contact time fluidized catalytic cracking process |
| GB8814292D0 (en) * | 1988-06-16 | 1988-07-20 | Shell Int Research | Process for conversion of hydrocarbonaceous feedstock |
| ES2087073T3 (en) * | 1988-06-16 | 1996-07-16 | Shell Int Research | PROCEDURE FOR THE CONVERSION OF A HYDROCARBON FEEDING MATERIAL. |
| NL8801653A (en) * | 1988-06-29 | 1990-01-16 | Stork Kwant Bv | OPERATING SYSTEM. |
| GB8828206D0 (en) * | 1988-12-02 | 1989-01-05 | Shell Int Research | Process for conversion of hydrocarbonaceous feedstock |
-
1989
- 1989-02-27 GB GB898904408A patent/GB8904408D0/en active Pending
-
1990
- 1990-02-14 CA CA002009986A patent/CA2009986A1/en not_active Abandoned
- 1990-02-21 ES ES90200415T patent/ES2056362T3/en not_active Expired - Lifetime
- 1990-02-21 DE DE69009234T patent/DE69009234T2/en not_active Revoked
- 1990-02-21 EP EP90200415A patent/EP0385538B1/en not_active Revoked
- 1990-02-22 BR BR909000880A patent/BR9000880A/en not_active Application Discontinuation
- 1990-02-23 AU AU50149/90A patent/AU628929B2/en not_active Ceased
- 1990-02-23 JP JP2041386A patent/JPH02276888A/en active Pending
- 1990-02-26 CN CN90100978A patent/CN1019981C/en not_active Expired - Fee Related
- 1990-02-26 RU SU904743371A patent/RU2017791C1/en active
- 1990-02-26 KR KR1019900002434A patent/KR910015689A/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| CN1045120A (en) | 1990-09-05 |
| DE69009234D1 (en) | 1994-07-07 |
| AU5014990A (en) | 1990-08-30 |
| BR9000880A (en) | 1991-02-13 |
| RU2017791C1 (en) | 1994-08-15 |
| EP0385538B1 (en) | 1994-06-01 |
| ES2056362T3 (en) | 1994-10-01 |
| KR910015689A (en) | 1991-09-30 |
| GB8904408D0 (en) | 1989-04-12 |
| JPH02276888A (en) | 1990-11-13 |
| DE69009234T2 (en) | 1994-11-24 |
| CN1019981C (en) | 1993-03-03 |
| AU628929B2 (en) | 1992-09-24 |
| EP0385538A1 (en) | 1990-09-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU743504B2 (en) | Two stage fluid catalytic cracking process for selectively producing c2 to c4 olefins | |
| US6977321B1 (en) | Production of propylene | |
| EP1036133B1 (en) | Production of olefins | |
| US5069776A (en) | Process for the conversion of a hydrocarbonaceous feedstock | |
| EP0372632A1 (en) | Process for the conversion of a hydrocarbonaceous feedstock | |
| EP0347003B1 (en) | Process for the conversion of a hydrocarbonaceous feedstock | |
| US5637207A (en) | Fluid catalytic cracking process | |
| JPH11246871A (en) | Production of olefin | |
| JPH11246872A (en) | Production of olefin | |
| US5278114A (en) | Hydrocarbon conversion process and catalyst composition | |
| EP0490435B1 (en) | Process for the preparation of an olefins-containing mixture of hydrocarbons | |
| US3801493A (en) | Slack wax cracking in an fccu with a satellite reactor | |
| CA1333375C (en) | Process for the conversion of a hydrocarbonaceous feedstock | |
| EP0385538B1 (en) | Process for the conversion of a hydrocarbonaceous feedstock | |
| EP0392590B1 (en) | Process for the conversion of a hydrocarbonaceous feedstock | |
| JPH1046160A (en) | Method for fluidized bed catalytic cracking of heavy oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| FZDE | Dead |