EP0512652A1 - Hydrodecyclization process - Google Patents
Hydrodecyclization process Download PDFInfo
- Publication number
- EP0512652A1 EP0512652A1 EP92201302A EP92201302A EP0512652A1 EP 0512652 A1 EP0512652 A1 EP 0512652A1 EP 92201302 A EP92201302 A EP 92201302A EP 92201302 A EP92201302 A EP 92201302A EP 0512652 A1 EP0512652 A1 EP 0512652A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- gas oil
- process according
- molar ratio
- type zeolite
- modified
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 31
- 239000003054 catalyst Substances 0.000 claims abstract description 12
- 125000004122 cyclic group Chemical group 0.000 claims abstract description 12
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 11
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000010457 zeolite Substances 0.000 claims abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000001257 hydrogen Substances 0.000 claims abstract description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 6
- 229910000510 noble metal Inorganic materials 0.000 claims abstract description 5
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 claims description 16
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 14
- 229930195733 hydrocarbon Natural products 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 9
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 8
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 7
- 229910052681 coesite Inorganic materials 0.000 claims description 7
- 229910052593 corundum Inorganic materials 0.000 claims description 7
- 229910052906 cristobalite Inorganic materials 0.000 claims description 7
- 239000000377 silicon dioxide Substances 0.000 claims description 7
- 235000012239 silicon dioxide Nutrition 0.000 claims description 7
- 229910052682 stishovite Inorganic materials 0.000 claims description 7
- 229910052905 tridymite Inorganic materials 0.000 claims description 7
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 7
- 150000001491 aromatic compounds Chemical class 0.000 claims description 5
- 229910052763 palladium Inorganic materials 0.000 claims description 4
- 229910052697 platinum Inorganic materials 0.000 claims description 4
- 239000003921 oil Substances 0.000 description 27
- 238000009835 boiling Methods 0.000 description 12
- 150000001875 compounds Chemical class 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 238000004517 catalytic hydrocracking Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
Definitions
- the present invention relates to a process for reducing the amount of cyclic structures present in a gas oil.
- Compounds contributing favourably to the cetane index are paraffins. Naphthenes contribute less favourably to the cetane index, while aromatics are even less desirable from that point of view.
- Several processes are known for increasing the cetane index of a given gas oil, such as hydrocracking and hydrogenation. Hydrocracking has as a disadvantage that part of the feed is converted into undesired lighter products. Hydrogenation comprises conversion of olefinic compounds, in particular aromatic compounds, into the corresponding saturated compounds. The optimum cetane index which is possible for a given gas oil without substantial cracking of molecules, will not be attained in this way.
- the present invention relates to a process for reducing the amount of cyclic structures present in a gas oil, which process comprises contacting a gas oil with hydrogen at elevated temperature and pressure using a catalyst comprising one or more Group VIII noble metal(s) on a support wherein the support comprises a modified Y-type zeolite having a unit cell size between 24.20 and 24.40 A and a SiO2/Al2O3 molar ratio of between 10 and 150 and recovering a gas oil comprising a reduced amount of cyclic structures.
- gas oil is meant a hydrocarbon oil comprising mainly hydrocarbons boiling in the range between 170 and 390 °C and containing at least 25% by weight of hydrocarbons boiling in the range between 250 and 390 °C, which hydrocarbon oil further has a cetane index between 38 and 49.
- a relatively light gas oil is used, i.e. mainly comprising hydrocarbons boiling in the range between 170 and 320 °C.
- hydrotreated gas oils are used as these have a relatively low nitrogen and sulphur content which contributes favourably to the life time of the catalyst.
- Hydrodecyclization is understood to comprise reduction of the amount of cyclic structures present in the gas oil.
- the amount of cyclic structures present is reduced with at least 10%, based on amount of cyclic structures present in the feed preferably with at least 15%.
- No substantial cracking takes place, which means that the gas oil recovered from the process according to the present invention comprises at least 5% by weight of hydrocarbons boiling in the range between the 90% by weight boiling point of the feed gas oil and the final boiling point of the feed gas oil.
- a catalyst comprising one or more Group VIII noble metal(s).
- Metals which can be suitably present are platinum and/or palladium.
- the catalyst comprises between 0.05 and 3% by weight of noble metal(s) based on amount of zeolite. More preferably, the catalyst comprises platinum and palladium in a molar ratio of between 0.25 and 0.75.
- the catalyst further comprises a support comprising a modified Y-type zeolite having a SiO2/Al2O3 molar ratio of between 10 and 150. It has been found that catalysts comprising a relatively low SiO2/Al2O3 molar ratio give surprisingly good results.
- a molar ratio which is preferred is between 15 and 50, more specifically between 20 and 45.
- the unit cell size of the Y-type zeolite applied is between 24.20 and 24.40 A, more specifically between 24.22 and 24.35.
- the hydrodecyclization process can suitably be carried out at a temperature between 150 and 400 °C, preferably at a temperature between 250 and 380 °C.
- the hydrogen partial pressure applied will usually be between 10 and 150 bar, preferably between 30 and 100 bar.
- the catalyst temperature and pressure will generally be chosen in such combination that a gas oil is produced having a cetane index of more than 45, preferably more than 50, and comprising less than 25% by weight of aromatic compounds, preferably less than 20. It was found that even gas oils having a cetane index of more than 50 and comprising less than 5% by weight of aromatic compounds, so-called “green gas oils", can be produced in the present process.
- the cetane index is measured according to ASTM D976.
- the characteristics of the gas oil produced depend on the feed gas oil and the process conditions.
- the cetane index and aromatic content which are aimed at in commercial operation, are determined by economic considerations.
- a hydrotreated straight run gas oil as described in Table 1 was contacted with a catalyst comprising Y-type zeolite having a unit cell size of 24.24 A and a SiO2/Al2O3 molar ratio of 40 and containing 0.3% by weight of platinum and 0.5% by weight of palladium, based on amount of zeolite, at a temperature of 265 °C, a hydrogen partial pressure of 35 bar and a weight hourly space velocity of 1.4 ton/m3.hour.
Landscapes
- Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Process for reducing the amount of cyclic structures present in a gas oil, which process comprises contacting a gas oil with hydrogen at elevated temperature and pressure using a catalyst comprising one or more Group VIII noble metal(s) on a support wherein the support comprises a modified Y-type zeolite.
Description
- The present invention relates to a process for reducing the amount of cyclic structures present in a gas oil.
- It is well known that hydrocarbon oil products have to fulfil certain chemical and physical requirements if they are to be commercially applied. One of the requirements a gas oil has to meet is the cetane index.
- Compounds contributing favourably to the cetane index are paraffins. Naphthenes contribute less favourably to the cetane index, while aromatics are even less desirable from that point of view. Several processes are known for increasing the cetane index of a given gas oil, such as hydrocracking and hydrogenation. Hydrocracking has as a disadvantage that part of the feed is converted into undesired lighter products. Hydrogenation comprises conversion of olefinic compounds, in particular aromatic compounds, into the corresponding saturated compounds. The optimum cetane index which is possible for a given gas oil without substantial cracking of molecules, will not be attained in this way.
- Further, it is important from an environmental point of view to produce a gas oil comprising a small amount of aromatics.
- It has now been found that a gas oil of good cetane index and low aromatics content can be obtained in a commercially attractive way by subjecting the gas oil to a specific process for reducing the amount of cyclic structures in a gas oil. In such process, the cetane index of the compounds present are optimized while hydrocracking of the hydrocarbons, whereby undesirable lighter products are produced, is substantially prevented.
- The present invention relates to a process for reducing the amount of cyclic structures present in a gas oil, which process comprises contacting a gas oil with hydrogen at elevated temperature and pressure using a catalyst comprising one or more Group VIII noble metal(s) on a support wherein the support comprises a modified Y-type zeolite having a unit cell size between 24.20 and 24.40 A and a SiO2/Al2O3 molar ratio of between 10 and 150 and recovering a gas oil comprising a reduced amount of cyclic structures.
- With gas oil is meant a hydrocarbon oil comprising mainly hydrocarbons boiling in the range between 170 and 390 °C and containing at least 25% by weight of hydrocarbons boiling in the range between 250 and 390 °C, which hydrocarbon oil further has a cetane index between 38 and 49. Suitably a relatively light gas oil is used, i.e. mainly comprising hydrocarbons boiling in the range between 170 and 320 °C. Preferably, hydrotreated gas oils are used as these have a relatively low nitrogen and sulphur content which contributes favourably to the life time of the catalyst.
- Hydrodecyclization is understood to comprise reduction of the amount of cyclic structures present in the gas oil. Preferably, the amount of cyclic structures present is reduced with at least 10%, based on amount of cyclic structures present in the feed preferably with at least 15%. No substantial cracking takes place, which means that the gas oil recovered from the process according to the present invention comprises at least 5% by weight of hydrocarbons boiling in the range between the 90% by weight boiling point of the feed gas oil and the final boiling point of the feed gas oil.
- In the process according to the present invention use is made of a catalyst comprising one or more Group VIII noble metal(s). Metals which can be suitably present are platinum and/or palladium. Preferably, the catalyst comprises between 0.05 and 3% by weight of noble metal(s) based on amount of zeolite. More preferably, the catalyst comprises platinum and palladium in a molar ratio of between 0.25 and 0.75.
- The catalyst further comprises a support comprising a modified Y-type zeolite having a SiO2/Al2O3 molar ratio of between 10 and 150. It has been found that catalysts comprising a relatively low SiO2/Al2O3 molar ratio give surprisingly good results. A molar ratio which is preferred is between 15 and 50, more specifically between 20 and 45. The unit cell size of the Y-type zeolite applied is between 24.20 and 24.40 A, more specifically between 24.22 and 24.35.
- The hydrodecyclization process can suitably be carried out at a temperature between 150 and 400 °C, preferably at a temperature between 250 and 380 °C. The hydrogen partial pressure applied will usually be between 10 and 150 bar, preferably between 30 and 100 bar.
- In the present process the catalyst, temperature and pressure will generally be chosen in such combination that a gas oil is produced having a cetane index of more than 45, preferably more than 50, and comprising less than 25% by weight of aromatic compounds, preferably less than 20. It was found that even gas oils having a cetane index of more than 50 and comprising less than 5% by weight of aromatic compounds, so-called "green gas oils", can be produced in the present process. The cetane index is measured according to ASTM D976.
- The characteristics of the gas oil produced depend on the feed gas oil and the process conditions. The cetane index and aromatic content which are aimed at in commercial operation, are determined by economic considerations.
- The process of the present invention will be further elucidated by the following example.
- A hydrotreated straight run gas oil as described in Table 1, was contacted with a catalyst comprising Y-type zeolite having a unit cell size of 24.24 A and a SiO2/Al2O3 molar ratio of 40 and containing 0.3% by weight of platinum and 0.5% by weight of palladium, based on amount of zeolite, at a temperature of 265 °C, a hydrogen partial pressure of 35 bar and a weight hourly space velocity of 1.4 ton/m³.hour.
- The results obtained are shown in Table 2.
- The amount of cyclic structures present in the product obtained was reduced with 18%, based on amount of cyclic structures present in the feed.
Table 1 Boiling point distribution (°C) Initial boiling point 179 10% 205 30% 218 50% 233 70% 249 90% 272 Final boiling point 294 Cetane index 49.3 Aromatics content (% by volume) 20.1 Table 2 Boiling point distribution (°C) Initial boiling point 180 10% 205 30% 218 50% 231 70% 247 90% 272 Final boiling point 293 Cetane index 53.4 Aromatics content (% by volume) 3.9
Claims (10)
- Process for reducing the amount of cyclic structures present in a gas oil, which process comprises contacting a gas oil with hydrogen at elevated temperature and pressure using a catalyst comprising one or more Group VIII noble metal(s) on a support wherein the support comprises a modified Y-type zeolite having a unit cell size between 24.20 and 24.40 A and a SiO2/Al2O3 molar ratio of between 10 and 150 and recovering a gas oil comprising a reduced amount of cyclic structures.
- Process according to claim 1, in which the modified Y-type zeolite has a SiO2/Al2O3 molar ratio of between 15 and 50.
- Process according to claim 2, in which the modified Y-type zeolite has a SiO2/Al2O3 molar ratio of between 20 and 45.
- Process according to any one of the preceding claims, in which the modified Y-type zeolite has a unit cell size of between 24.22 and 24.35 A.
- Process according to any one of the preceding claims, in which the process is carried out at a temperature between 150 and 400 °C.
- Process according to any one of the preceding claims, in which the process is carried out at a hydrogen partial pressure between 10 and 150 bar.
- Process according to any one of the preceding claims, in which the catalyst comprises platinum and palladium in a molar ratio of between 0.25 to 0.75.
- Process according to any one of the preceding claims, in which a gas oil is recovered comprising less than 25% by weight of aromatic compounds and having a cetane index of more than 50.
- Process according to any one of the preceding claims, in which a gas oil is recovered comprising less than 5% by weight of aromatic compounds and having a cetane index of more than 50.
- Hydrocarbons obtained in a process as described in any one of the preceding claims.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB919110012A GB9110012D0 (en) | 1991-05-09 | 1991-05-09 | Hydrodecyclization process |
| GB9110012 | 1991-05-09 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0512652A1 true EP0512652A1 (en) | 1992-11-11 |
| EP0512652B1 EP0512652B1 (en) | 1995-08-23 |
Family
ID=10694685
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP92201302A Expired - Lifetime EP0512652B1 (en) | 1991-05-09 | 1992-05-07 | Hydrodecyclization process |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0512652B1 (en) |
| JP (1) | JP3210729B2 (en) |
| CA (1) | CA2068174C (en) |
| DE (1) | DE69204206T2 (en) |
| DK (1) | DK0512652T3 (en) |
| ES (1) | ES2077338T3 (en) |
| FI (1) | FI114317B (en) |
| GB (1) | GB9110012D0 (en) |
| NO (1) | NO304029B1 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001027223A1 (en) * | 1999-10-13 | 2001-04-19 | Veba Oil Refining & Petrochemicals Gmbh | Method for production of n-alkanes from mineral oil fractions and catalyst for carrying out said method |
| US6399845B1 (en) | 1997-05-29 | 2002-06-04 | Fortum Oil & Gas Oy | Process for producing high grade diesel fuel |
| US6444865B1 (en) | 1997-12-01 | 2002-09-03 | Shell Oil Company | Process wherein a hydrocarbon feedstock is contacted with a catalyst |
| US7709408B2 (en) * | 2002-07-16 | 2010-05-04 | Consejo Superior De Investigaciones Cientificas | Catalyst based on a solid microporous crystalline material and method of improving diesel fraction quality using said catalyst |
| CN105713657A (en) * | 2014-12-01 | 2016-06-29 | 中国石油化工股份有限公司 | Hydrocracking method |
| WO2017148735A1 (en) | 2016-03-01 | 2017-09-08 | Sabic Global Technologies B.V. | Process for producing monoaromatic hydrocarbons from a hydrocarbon feed comprising polyaromatics |
| US11001765B2 (en) | 2016-02-25 | 2021-05-11 | Sabic Global Technologies B.V. | Process for combined hydrodesulfurization and hydrocracking of heavy hydrocarbons |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100438816B1 (en) * | 1998-03-09 | 2004-07-16 | 삼성전자주식회사 | Personal solid image head mount display device, especially including two dimensional image display |
| KR100419288B1 (en) * | 2001-06-22 | 2004-02-19 | 인천정유 주식회사 | Method for preparing catalysts for dearomatization in distillate |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0247678A2 (en) * | 1986-05-30 | 1987-12-02 | Shell Internationale Researchmaatschappij B.V. | Hydrocarbon conversion process and catalysts |
-
1991
- 1991-05-09 GB GB919110012A patent/GB9110012D0/en active Pending
-
1992
- 1992-05-07 DE DE69204206T patent/DE69204206T2/en not_active Expired - Fee Related
- 1992-05-07 FI FI922069A patent/FI114317B/en active IP Right Grant
- 1992-05-07 DK DK92201302.4T patent/DK0512652T3/en active
- 1992-05-07 EP EP92201302A patent/EP0512652B1/en not_active Expired - Lifetime
- 1992-05-07 NO NO921806A patent/NO304029B1/en unknown
- 1992-05-07 ES ES92201302T patent/ES2077338T3/en not_active Expired - Lifetime
- 1992-05-07 JP JP14110192A patent/JP3210729B2/en not_active Expired - Fee Related
- 1992-05-07 CA CA002068174A patent/CA2068174C/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0247678A2 (en) * | 1986-05-30 | 1987-12-02 | Shell Internationale Researchmaatschappij B.V. | Hydrocarbon conversion process and catalysts |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6399845B1 (en) | 1997-05-29 | 2002-06-04 | Fortum Oil & Gas Oy | Process for producing high grade diesel fuel |
| US6444865B1 (en) | 1997-12-01 | 2002-09-03 | Shell Oil Company | Process wherein a hydrocarbon feedstock is contacted with a catalyst |
| WO2001027223A1 (en) * | 1999-10-13 | 2001-04-19 | Veba Oil Refining & Petrochemicals Gmbh | Method for production of n-alkanes from mineral oil fractions and catalyst for carrying out said method |
| US7067448B1 (en) | 1999-10-13 | 2006-06-27 | Veba Oil Refining And Petrochemicals Gmbh | Method for production of n-alkanes from mineral oil fractions and catalyst for carrying out said method |
| CZ297150B6 (en) * | 1999-10-13 | 2006-09-13 | Veba Oil Refining & Petrochemicals Gmbh | Process for preparing n-alkanes, catalyst for making the process and use of such a catalyst |
| US7709408B2 (en) * | 2002-07-16 | 2010-05-04 | Consejo Superior De Investigaciones Cientificas | Catalyst based on a solid microporous crystalline material and method of improving diesel fraction quality using said catalyst |
| CN105713657A (en) * | 2014-12-01 | 2016-06-29 | 中国石油化工股份有限公司 | Hydrocracking method |
| CN105713657B (en) * | 2014-12-01 | 2017-05-17 | 中国石油化工股份有限公司 | Hydrocracking method |
| US11001765B2 (en) | 2016-02-25 | 2021-05-11 | Sabic Global Technologies B.V. | Process for combined hydrodesulfurization and hydrocracking of heavy hydrocarbons |
| WO2017148735A1 (en) | 2016-03-01 | 2017-09-08 | Sabic Global Technologies B.V. | Process for producing monoaromatic hydrocarbons from a hydrocarbon feed comprising polyaromatics |
| CN108699449A (en) * | 2016-03-01 | 2018-10-23 | 沙特基础工业全球技术有限公司 | Method for producing mononuclear aromatics by the hydrocarbon charging comprising polycyclic aromatic hydrocarbon |
| US10822552B2 (en) | 2016-03-01 | 2020-11-03 | Sabic Global Technologies B.V. | Process for producing monoaromatic hydrocarbons from a hydrocarbon feed comprising polyaromatics |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2068174A1 (en) | 1992-11-10 |
| NO921806D0 (en) | 1992-05-07 |
| CA2068174C (en) | 2003-12-02 |
| JPH05179260A (en) | 1993-07-20 |
| DE69204206D1 (en) | 1995-09-28 |
| NO304029B1 (en) | 1998-10-12 |
| JP3210729B2 (en) | 2001-09-17 |
| DK0512652T3 (en) | 1995-09-25 |
| ES2077338T3 (en) | 1995-11-16 |
| FI922069A (en) | 1992-11-10 |
| EP0512652B1 (en) | 1995-08-23 |
| FI922069A0 (en) | 1992-05-07 |
| FI114317B (en) | 2004-09-30 |
| DE69204206T2 (en) | 1996-02-01 |
| GB9110012D0 (en) | 1991-07-03 |
| NO921806L (en) | 1992-11-10 |
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