EP0372632B1 - Kohlenwasserstoffumwandlungsverfahren - Google Patents

Kohlenwasserstoffumwandlungsverfahren Download PDF

Info

Publication number
EP0372632B1
EP0372632B1 EP19890203038 EP89203038A EP0372632B1 EP 0372632 B1 EP0372632 B1 EP 0372632B1 EP 19890203038 EP19890203038 EP 19890203038 EP 89203038 A EP89203038 A EP 89203038A EP 0372632 B1 EP0372632 B1 EP 0372632B1
Authority
EP
European Patent Office
Prior art keywords
feedstock
catalyst
process according
zeolite
carried out
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.)
Revoked
Application number
EP19890203038
Other languages
English (en)
French (fr)
Other versions
EP0372632A1 (de
Inventor
Ian Ernest Maxwell
Jaydeep Biswas
Johannes Kornelis Minderhoud
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=10647877&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP0372632(B1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0372632A1 publication Critical patent/EP0372632A1/de
Application granted granted Critical
Publication of EP0372632B1 publication Critical patent/EP0372632B1/de
Anticipated expiration legal-status Critical
Revoked legal-status Critical Current

Links

Images

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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen

Definitions

  • the present invention relates to a process for the conversion of a hydrocarbonaceous feedstock and is particularly concerned with the upgrading of certain feedstocks.
  • 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.
  • US 4,502,945 describes a dewaxing process for upgrading a paraffinic hydrocarbonaceous feedstock by contacting the feedstock with an intermediate pore size zeolite at a pressure of 1 to 8 bar, a temperature of 290 to 595C, preferably of 340 to 480C, and a space velocity of 0.1 to 50 v/v/hr.
  • the zeolite must have a silica:alumina mole ratio from about 175:1 to about 300:1 and is preferably ZSM-5.
  • the upgraded product includes olefinic hydrocarbons such as propene and butenes.
  • US 3,856,659 describes a multistage hydrocarbon conversion operation in the presence of a dual cracking catalyst composition comprising ZSM-5 material, for the production of gasoline and olefinic components, employing one or more riser reactors in parallel flow arrangement wherein the larger and smaller pore catalytic cracking materials comprising the dual function catalyst work substantially independently in their restructuring of hydrocarbon constituents coming in contact therewith under particularly selected operating conditions.
  • a first hydrocarbon feed contacts the dual function catalyst in a riser conversion zone
  • the dual function Catalyst is then contacted with a second hydrocarbon feed more refractory than the first under conditions to substantially deactivate the cracking activity of the large pore catalyst component without undesirably influencing the activity of the small pore catalyst component which can then be contacted with low boiling hydrocarbon components to effect their restructuring to cyclic components of relatively high octane rating.
  • the present invention provides a process for the conversion of a hydrotreated and/or hydrocracked heavy hydrocarbonaceous feedstock to obtain a high proportion of olefinically unsaturated gaseous products, which process comprises contacting the feedstock in a single stage with a zeolitic catalyst comprising a zeolite with a pore diameter of 0.4 to 0.7 nm wherein the contacting is carried out at a catalyst/feedstock weight ratio from 2 to 200, a temperature of greater than or equal to 480 °C and a pressure of up to 10 bar during less than 10 seconds.
  • the feedstock is contacted with the zeolitic catalyst for less than 10 seconds.
  • 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 1 to 6 seconds.
  • the temperature during the reaction is relatively high. However, the combination of high temperature and short residence time allows a high conversion to olefins.
  • a preferred temperature range is 480 to 900 °C, more preferably 500 to 750 °C.
  • the zeolitic catalyst comprises a zeolite with a pore diameter of from 0.4 to 0.7 nm.
  • the catalyst suitably further comprises a refractory oxide that serves as binder material. Suitable 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 50:50 to 85:15.
  • the catalyst may comprise further zeolites with a pore diameter above 0.7 nm.
  • zeolites include the faujasite-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 diameter of from 0.4 to 0.7 nm.
  • 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 0.4 to 0.7 nm include SAPO-4 and SAPO-11, which are described in US-A-4,440,871, ALPO-11, described in US-A-4,310,440, TAPO-11, 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 zeolites such as ZSM-5, ZSM-11, ZSM-12, ZSM-35, ZSM-23, and ZSM-38.
  • SAPO-4 and SAPO-11 which are described in US-A-4,440,871, ALPO-11, described in US-A-4,310,440, TAPO-11, described in US-A-4,500,651, TASO-45, described in EP-A-229,29
  • the zeolite is selected from the group consisting of crystalline metal silicates having a ZSM-5 structure, ferrierite, erionite and mixtures thereof.
  • crystalline metal silicates with ZSM-5 structure are aluminium, gallium, iron, scandium, rhodium and/or scandium silicates as described in e.g. GB-B-2,110,559.
  • the zeolites usually a significant amount of alkali metal oxide is present in the prepared zeolite.
  • 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.
  • the zeolite used in the present process is substantially in its hydrogen form.
  • Olefin production is facilitated by the absence of hydrogen or a hydrogen donor.
  • the present process is advantageously carried out in the absence of added hydrogen and/or steam. It is, of course, possible that during the reaction some small molecules, such as hydrogen molecules are formed. However, this amount is usually negligible and will be less than 0.5 %wt of the product.
  • 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. Then it is easier to achieve the short contact times envisaged. Hence, the pressure is preferably relatively low. This is the more advantageous since no expensive compressors and high-pressure vessels and other equipment are necessary. Pressures up to 10 bar can be employed. Subatmospheric pressures are possible, but not preferred. The minimum pressure is suitably 1 bar. It is economically advantageous to operate at atmospheric pressure.
  • the catalyst/feedstock weight ratio may vary widely, for example up to 200 kg of catalyst per kg of feedstock. Preferably, the catalyst/feedstock weight ratio is from 2 to 200.
  • the process according to the present invention may be carried out in a fixed bed. However, this would imply that extremely high space velocities be required to attain the short contact times envisaged. Therefore, the present process is preferably carried out in a moving bed.
  • the bed of catalyst may move upwards or downwards. When the bed moves upwards a process similar to a fluidized catalytic cracking process is obtained. Preferably, the process is carried out in a downwardly moving bed.
  • the catalyst is regenerated by subjecting it, after having been contacted with the feedstock, to a treatment with an oxidizing gas, such as air.
  • a continuous regeneration similar to the regeneration carried out in a fluidized catalytic cracking process, is especially preferred.
  • the coke formation does not occur at a very high rate.
  • 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.
  • the residence time of the catalyst is from 1 to 20 times the residence time of the feedstock.
  • the feedstock which is to be converted in the present process comprises hydrotreated and/or hydrocracked hydrocarbons, preferably, though not necessarily, heavy feedstocks.
  • Suitable feedstocks are obtained by hydrotreating and/or hydrocracking heavy flashed distillate fractions from long residue or deasphalted oils obtained from short residue.
  • the feedstock is suitably fractionated to remove lower boiling fractions after hydrotreating and/or hydrocracking and prior to contacting with the zeolitic catalyst in accordance with the invention.
  • the product obtained by the process of the invention is optionally fractionated to yield an olefin-rich gas fraction, a gasoline fraction and a bottom fraction, all or part of which is optionally recycled to the feedstock upstream of the hydrotreating and/or hydrocracking unit. In this way, high conversion of the heavy deasphalted oil or heavy flashed discillate feedstock to more valuable olefin-rich gas is obtained.
  • a process for the conversion of a hydrocarbonaceous feedstock comprising hydrotreating and/or hydrocracking said feedstock in the presence of a suitable catalyst, contacting at least a part of the hydrotreated and/or hydrocracked product with a zeolitic catalyst comprising a zeolite with a pore diameter of 0.4 to 0.7 nm at a temperature of greater than 480 °C and a pressure of up to 10 bar during less than 10 seconds, fractionating the resulting converted material and recycling a heavier fraction to said hydrotreating and/or hydrocracking step.
  • the said hydrotreating step is known in the art and may be carried out at known conditions. Suitable conditions include a temperature of 150 to 400 °C, a hydrogen (partial) pressure of 30 to 150 bar, a space velocity of 0.5 to 4.0 kg/l.h and a hydrogen/feedstock ratio of 100 to 2000 Nl/kg.
  • Suitable hydrotreating catalysts- comprise nickel, cobalt, tungsten, molybdenum, platinum, palladium or mixtures thereof on a carrier, such as alumina, silica-alumina, silica, zirconia, zeolites and the like.
  • the catalyst may further comprise fluorine, phosphorus and/or boron.
  • the temperature, gas rate and space velocity can be selected by the person skilled in the art, suitably from the range given above.
  • Hydrocracking is also known in the art and may be carried out under known conditions, such as over a hydrocracking catalyst at a temperature of 300 to 450 °C, a hydrogen (partial) pressure of 50 to 200 bar, a space velocity of 0.5 to 2.0 kg/l.catalyst.h and a H2/mineral oil fraction ratio of 500 to 2000 Nl/kg.
  • the hydrocracking catalyst can be selected from any hydrocracking catalyst known in the art.
  • the hydrocracking catalyst comprises a carrier and at least one hydrogenating metal or a compound thereof, which carrier has been selected from the group consisting of silica, alumina, silica-alumina and the faujasite-type zeolites.
  • the most preferred faujasite-type zeolite is zeolite Y.
  • the most preferred hydrogenating metals are nickel, cobalt, tungsten and molybdenum and mixtures thereof, but platinum and/or palladium may also be used.
  • the catalyst may further comprise fluorine and/or phosphorus and/or boron.
  • nickel, cobalt, molybdenum and/or tungsten are used as hydrogenating metal, they are preferably present in the form of their sulphides.
  • a feedstock with a nitrogen content greater than 5 ppmw may be used with substantially no effect on the catalyst activity.
  • Suitable feedstocks may have a nitrogen content of more than 10 ppmw, calculated as nitrogen.
  • the feedstock may even have a nitrogen content of 1000 ppmw or more, calculated as nitrogen.
  • the feedstock in this example was a hydrotreated Arabian light deasphalted oil having the following properties: IBP, °C 453 50 %wt 591 67 %wt 620 density 70/4 0.8532 kg/l sulphur 232 ppmw nitrogen 12 ppmw
  • the DAO feedstock was upgraded in a downflow reactor by passing it downwards co-currently with a flow of catalyst particles.
  • the catalyst comprised ZSM-5 in an alumina matrix (weight ratio ZSM-5/alumina 1:3).
  • the experiment was carried out at atmospheric pressure. Further process conditions and the results of the experiment are given in Table 1 below.
  • the feedstock in this example was a hydrocracked heavy flashed distillate having the following properties: IBP, °C 330 50 %wt 432 FBP, °C 620 fraction boiling below 370 °C, %wt 7.7 density 70/4 0.8157 kg/l sulphur 20 ppmw nitrogen 2 ppmw
  • Feedstock was introduced on line 1, after mixing with hydrogen from line 2, to a hydrotreating/hydrocracking unit 3 operated at 90 bar hydrogen partial pressure at 400 °C with a suitable Ni/Mo/alumina hydrotreating cacalyst.
  • the hydrotreated product was fractionated in unit 4 into a gaseous fraction 5, a naphtha fraction 6, a kerosine fraction 7, a gas oil fraction 8 and a bottoms fraction 9.
  • bottoms fraction 9 was passed to a downflow reactor 10 as described in Example 1, containing catalyst as described in Example 1 and provided with suitable regeneration means from which coke can be removed in line 11 when necessary, while gaseous and liquid product is separated in fractionation unit 12 into a gaseous product 13, a gasoline product 14 and a bottoms stream 15, which is recycled to the feedstock in line 1 for re-processing.
  • Bottoms fraction 9 which is upgraded in reactor 10 comprises about 69% by weight based on the initial feed in line 1 when fractionated in unit 12.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)

Claims (9)

  1. Verfahren für die Umwandlung eines wasserstoffbehandelten und/oder wasserstoffgecrackten kohlenwasserstoffhaltigen Ausgangsmaterials, um einen hohen Anteil an olefinisch ungesättigten gasförmigen Produkten zu erhalten, bei dem man das Ausgangsmaterial in einem einzigen Schritt mit einem zeolithischen Katalysator aus einem Zeolithen mit einem Porendurchmesser von 0,4 bis 0,7 nm kontaktiert, dadurch gekennzeichnet, daß man die Kontaktbehandlung bei einem Katalysator/Ausgangsmaterial-Gewichtsverhältnis von 2 bis 200, einer Temperatur von 480°C oder höher und einem Druck von bis zu 10 bar innerhalb von weniger als 10 Sekunden durchführt.
  2. Verfahren nach Anspruch 1, in dem man das Ausgangsmaterial mit dem zeolithischen Katalysator innerhalb von ein bis 6 Sekunden kontaktiert.
  3. Verfahren nach Anspruch 1 oder 2, in dem die Temperatur zwischen 480 und 900°C liegt.
  4. Verfahren nach einem der vorhergehenden Ansprüche, bei dem man den Zeolithen aus kristallinen Metallsilikaten mit ZSM-5-Struktur, Ferrierit, Erionit und deren Gemischen auswählt.
  5. Verfahren nach einem der vorhergehenden Ansprüche, in dem der Zeolith überwiegend in seiner Wasserstofform vorliegt.
  6. Verfahren nach einem der vorhergehenden Ansprüche, das man ohne Wasserstoff- oder Dampfzusatz durchführt.
  7. Verfahren nach einem der vorhergehenden Ansprüche, das man in einem von unten nach oben oder von oben nach unten wanderuden Wanderbett durchführt.
  8. Verfahren nach einem der vorhergehenden Ansprüche, bei dem das Ausgangsmaterial ein wasserstoffbehandeltes und/oder wasserstoffgecracktes entasphaltiertes Öl oder schweres Vakuumdestillat ist.
  9. Verfahren nach einem der vorhergehenden Ansprüche, bei dem man das Ausgangsmaterial zunächst einer Wasserstoffbehandlung und/oder einem Wasserstoffcracken in Gegenwart eines geeigneten Katalysators unterzieht, das nach dem Verfahren eines der vorhergehenden Ansprüche umgewandelte Material fraktioniert und die schwerere Fraktion wieder besagter Wasserstoffbehandlung und/oder besagtem Wasserstoffcracken zuführt.
EP19890203038 1988-12-02 1989-11-29 Kohlenwasserstoffumwandlungsverfahren Revoked EP0372632B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8828206 1988-12-02
GB888828206A GB8828206D0 (en) 1988-12-02 1988-12-02 Process for conversion of hydrocarbonaceous feedstock

Publications (2)

Publication Number Publication Date
EP0372632A1 EP0372632A1 (de) 1990-06-13
EP0372632B1 true EP0372632B1 (de) 1996-01-31

Family

ID=10647877

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19890203038 Revoked EP0372632B1 (de) 1988-12-02 1989-11-29 Kohlenwasserstoffumwandlungsverfahren

Country Status (11)

Country Link
EP (1) EP0372632B1 (de)
JP (1) JPH02212594A (de)
CN (1) CN1025216C (de)
AU (1) AU621169B2 (de)
BR (1) BR8906158A (de)
CA (1) CA2004390A1 (de)
DE (1) DE68925574T2 (de)
ES (1) ES2082769T3 (de)
GB (1) GB8828206D0 (de)
PH (1) PH27238A (de)
RU (1) RU2017790C1 (de)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
US7833926B2 (en) 2005-07-01 2010-11-16 Sk Energy Co., Ltd. Arylphenoxy catalyst system for producing ethylene homopolymer or copolymers of ethylene and α-olefins
US10689586B2 (en) 2015-12-21 2020-06-23 Sabic Global Technologies B.V. Methods and systems for producing olefins and aromatics from coker naphtha
KR20240045992A (ko) 2022-09-30 2024-04-08 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 전이금속 화합물, 이를 포함하는 촉매 조성물 및 이를 이용하는 올레핀 중합체의 제조방법

Families Citing this family (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB8904408D0 (en) * 1989-02-27 1989-04-12 Shell Int Research Process for the conversion of a hydrocarbonaceous feedstock
CN1034223C (zh) * 1993-03-29 1997-03-12 中国石油化工总公司 制取低碳烯烃的裂解催化剂
CN1034586C (zh) * 1993-11-05 1997-04-16 中国石油化工总公司 多产低碳烯烃的催化转化方法
FR2778345B1 (fr) * 1998-05-06 2000-11-24 Inst Francais Du Petrole Catalyseur a base de zeolithe y contenant du bore et/ou du silicium, utilisable en hydrocraquage
FR2778343B1 (fr) 1998-05-06 2000-06-16 Inst Francais Du Petrole Catalyseur a base de zeolithe y non globalement desaluminee, de bore et/ou de silicium et procede d'hydrocraquage
FR2778582B1 (fr) * 1998-05-13 2000-06-16 Inst Francais Du Petrole Procede pour l'amelioration du point d'ecoulement et catalyseur a base d'au moins une zeolithe mtt, ton, fer
CN101210200B (zh) 2006-12-27 2010-10-20 中国石油化工股份有限公司 一种渣油加氢处理与催化裂化组合工艺方法
JP5840840B2 (ja) 2007-12-20 2016-01-06 中国石油化工股▲分▼有限公司 炭化水素油を水素化し接触分解するための、改善された一体的方法
KR101151606B1 (ko) 2007-12-31 2012-06-08 에스케이이노베이션 주식회사 전이금속 화합물, 이를 포함하는 촉매조성물 및 이를이용한 올레핀 단독중합 또는 공중합체의 제조방법
KR101186489B1 (ko) 2008-01-07 2012-09-27 에스케이이노베이션 주식회사 전이금속 화합물 및 이를 포함하는 에틸렌 단독중합체 또는공중합체 제조용 전이금속 촉매 조성물
KR101142115B1 (ko) 2008-01-07 2012-07-06 에스케이이노베이션 주식회사 전이금속 화합물, 이를 포함하는 전이금속 촉매 조성물, 및이를 이용한 에틸렌 단독중합체 또는 에틸렌과α-올레핀의 공중합체의 제조방법
KR101142117B1 (ko) 2008-09-25 2012-05-09 에스케이이노베이션 주식회사 전이금속 촉매계 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체 제조방법
KR101167082B1 (ko) 2008-11-05 2012-07-20 에스케이이노베이션 주식회사 에틸렌과 α-올레핀의 탄성 공중합체 제조방법
KR101212637B1 (ko) 2011-06-09 2012-12-14 에스케이종합화학 주식회사 신규한 사이클로펜타［ｂ］플루오레닐 전이금속 화합물, 이를 포함하는 전이금속 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
CA2801839C (en) 2011-06-24 2019-07-02 Sk Innovation Co., Ltd. Advanced transition metal catalytic systems in terms of comonomer incorporations and methods for preparing ethylene homopolymers or copolymers of ethylene and .alpha.-olefins using the same
KR102300853B1 (ko) 2014-05-29 2021-09-13 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 새로운 전이금속 화합물, 이를 포함한 올레핀 중합용 전이금속 촉매 조성물 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
KR102038977B1 (ko) 2016-12-30 2019-11-01 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 신규한 시클로펜타[ｂ]티오펜일 전이금속 화합물, 이를 포함하는 전이금속 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
KR101980683B1 (ko) 2017-01-06 2019-05-22 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 신규한 인덴계 전이금속 화합물, 이를 포함하는 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
KR102034133B1 (ko) 2017-01-09 2019-11-18 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 신규한 전이금속 화합물, 이를 포함하는 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
KR102100134B1 (ko) 2017-08-21 2020-04-13 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 신규한 전이금속 화합물, 이를 포함하는 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
KR102643986B1 (ko) 2017-09-29 2024-03-07 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 신규한 인덴계 전이금속 화합물, 이를 포함하는 전이금속 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
WO2019064247A1 (ko) 2017-09-29 2019-04-04 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 신규한 인덴계 전이금속 화합물, 이를 포함하는 전이금속 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
WO2019123028A1 (ko) 2017-12-21 2019-06-27 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 금속-리간드 착체, 이를 포함하는 에틸렌계 중합용 촉매 조성물 및 이를 이용한 에틸렌계 중합체의 제조방법
KR102100142B1 (ko) 2017-12-21 2020-04-14 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 금속-리간드 착체, 이를 포함하는 에틸렌계 중합용 촉매 조성물 및 이를 이용한 에틸렌계 중합체의 제조방법
KR102714698B1 (ko) 2019-02-28 2024-10-10 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 신규한 테트라아릴보레이트 화합물, 이를 포함하는 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
WO2020174346A1 (ko) 2019-02-28 2020-09-03 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 신규한 테트라아릴보레이트 화합물, 이를 포함하는 촉매 조성물, 및 이를 이용한 에틸렌 단독중합체 또는 에틸렌과 α-올레핀의 공중합체의 제조방법
JP7394222B2 (ja) 2019-12-03 2023-12-07 サビック エスケー ネクスレン カンパニー ピーティーイー リミテッド 遷移金属化合物、これを含む触媒組成物およびこれを用いるオレフィン重合体の製造方法

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3420770A (en) * 1966-09-28 1969-01-07 Mobil Oil Corp Catalytic cracking of hydrocarbons
US3856659A (en) * 1972-12-19 1974-12-24 Mobil Oil Corp Multiple reactor fcc system relying upon a dual cracking catalyst composition
US4171257A (en) * 1978-10-23 1979-10-16 Chevron Research Company Petroleum distillate upgrading process
US4502945A (en) * 1982-06-09 1985-03-05 Chevron Research Company Process for preparing olefins at high pressure
NL8301352A (nl) * 1983-04-18 1984-11-16 Shell Int Research Werkwijze voor de bereiding van asfaltenenarme koolwaterstofmengsels.
EP0125709B1 (de) * 1983-04-18 1989-08-02 Shell Internationale Researchmaatschappij B.V. Verfahren zur Herstellung von Kohlenwasserstoffgemischen mit niedrigem Asphaltgehalt
BR8902859A (pt) * 1988-06-16 1990-02-01 Shell Int Research Processo para conversao de uma carga de alimentacao hidrocarbonada e produto hidrocarbonado

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
US7833926B2 (en) 2005-07-01 2010-11-16 Sk Energy Co., Ltd. Arylphenoxy catalyst system for producing ethylene homopolymer or copolymers of ethylene and α-olefins
US10689586B2 (en) 2015-12-21 2020-06-23 Sabic Global Technologies B.V. Methods and systems for producing olefins and aromatics from coker naphtha
KR20240045992A (ko) 2022-09-30 2024-04-08 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 전이금속 화합물, 이를 포함하는 촉매 조성물 및 이를 이용하는 올레핀 중합체의 제조방법

Also Published As

Publication number Publication date
CA2004390A1 (en) 1990-06-02
GB8828206D0 (en) 1989-01-05
CN1025216C (zh) 1994-06-29
ES2082769T3 (es) 1996-04-01
CN1043156A (zh) 1990-06-20
PH27238A (en) 1993-05-04
BR8906158A (pt) 1990-07-31
RU2017790C1 (ru) 1994-08-15
JPH02212594A (ja) 1990-08-23
EP0372632A1 (de) 1990-06-13
AU4579989A (en) 1990-06-07
DE68925574D1 (de) 1996-03-14
AU621169B2 (en) 1992-03-05
DE68925574T2 (de) 1996-08-08

Similar Documents

Publication Publication Date Title
EP0372632A1 (de) Kohlenwasserstoffumwandlungsverfahren
US4976847A (en) Process for the catalytic cracking of a hydrocarbon feedstock
US6149800A (en) Process for increased olefin yields from heavy feedstocks
US6123830A (en) Integrated staged catalytic cracking and staged hydroprocessing process
EP1205530B1 (de) Katalytisches umwandlungsverfahren zur herstellung von dieselöl und verflüssigtem gas
US5152883A (en) Process for the production of improved octane numbers gasolines
US4126538A (en) Process for the conversion of hydrocarbons
US20010042700A1 (en) Naphtha and cycle oil conversion process
JPH0135874B2 (de)
US20010027936A1 (en) Process for converting petroleum fractions, comprising an ebullated bed hydroconversion step, a separation step, a hydrodesulphurisation step and a cracking step
US5637207A (en) Fluid catalytic cracking process
EP0347003B1 (de) Verfahren zur Umwandlung einer Kohlenwasserstoffhaltigen Fraktion
US5770043A (en) Integrated staged catalytic cracking and hydroprocessing process
US4201659A (en) Process for the preparation of gas oil
US5770044A (en) Integrated staged catalytic cracking and hydroprocessing process (JHT-9614)
US4192734A (en) Production of high quality fuel oils
US4853105A (en) Multiple riser fluidized catalytic cracking process utilizing hydrogen and carbon-hydrogen contributing fragments
EP0490435B1 (de) Verfahren zur Herstellung eines Olefine enthaltenden Kohlenwasserstoffgemisches
EP0349036B1 (de) Verfahren zur Umwandlung eines kohlenwasserstoffartigen Ausgangsmaterials
EP0385538B1 (de) Verfahren zur Umwandlung von Kohlenwasserstoffen
EP0392590B1 (de) Verfahren zur Umwandlung einer Kohlenwasserstoffbeschickung
AU634612B2 (en) Process for preparing one or more light hydrocarbon oil distillates
Biswas et al. Octane Enhancement Induced by Zeolites in Fluid Catalytic Cracking

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): BE DE ES FR GB IT NL

17P Request for examination filed

Effective date: 19901016

17Q First examination report despatched

Effective date: 19910528

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE ES FR GB IT NL

REF Corresponds to:

Ref document number: 68925574

Country of ref document: DE

Date of ref document: 19960314

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2082769

Country of ref document: ES

Kind code of ref document: T3

ITF It: translation for a ep patent filed
ET Fr: translation filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19960926

Year of fee payment: 8

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19961018

Year of fee payment: 8

PLBQ Unpublished change to opponent data

Free format text: ORIGINAL CODE: EPIDOS OPPO

PLAV Examination of admissibility of opposition

Free format text: ORIGINAL CODE: EPIDOS OPEX

PLBI Opposition filed

Free format text: ORIGINAL CODE: 0009260

PLBQ Unpublished change to opponent data

Free format text: ORIGINAL CODE: EPIDOS OPPO

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19961105

Year of fee payment: 8

PLBQ Unpublished change to opponent data

Free format text: ORIGINAL CODE: EPIDOS OPPO

PLBI Opposition filed

Free format text: ORIGINAL CODE: 0009260

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 19961118

Year of fee payment: 8

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19961127

Year of fee payment: 8

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19961211

Year of fee payment: 8

26 Opposition filed

Opponent name: AKZO NOBEL N.V.

Effective date: 19961029

Opponent name: MOBIL OIL CORPORATION

Effective date: 19961029

26 Opposition filed

Opponent name: EXXON CHEMICAL TECHNICAL CENTRE

Effective date: 19961031

Opponent name: AKZO NOBEL N.V.

Effective date: 19961029

Opponent name: MOBIL OIL CORPORATION

Effective date: 19961029

NLR1 Nl: opposition has been filed with the epo

Opponent name: EXXON CHEMICAL TECHNICAL CENTRE

Opponent name: AKZO NOBEL N.V.

Opponent name: MOBIL OIL CORPORATION

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

RDAH Patent revoked

Free format text: ORIGINAL CODE: EPIDOS REVO

PLAB Opposition data, opponent's data or that of the opponent's representative modified

Free format text: ORIGINAL CODE: 0009299OPPO

PLBQ Unpublished change to opponent data

Free format text: ORIGINAL CODE: EPIDOS OPPO

R26 Opposition filed (corrected)

Opponent name: MOBIL OIL CORPORATION * 961029 AKZO NOBEL N.V. * 9

Effective date: 19961029

RDAG Patent revoked

Free format text: ORIGINAL CODE: 0009271

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: PATENT REVOKED

NLR1 Nl: opposition has been filed with the epo

Opponent name: EXXON CHEMICAL TECHNICAL CENTRE

Opponent name: AKZO NOBEL N.V.

Opponent name: MOBIL OIL CORPORATION

27W Patent revoked

Effective date: 19970823

GBPR Gb: patent revoked under art. 102 of the ep convention designating the uk as contracting state

Free format text: 970823

NLR2 Nl: decision of opposition