EP1453937B1 - Hydrocraquage a contre courant - Google Patents

Hydrocraquage a contre courant Download PDF

Info

Publication number
EP1453937B1
EP1453937B1 EP02787711A EP02787711A EP1453937B1 EP 1453937 B1 EP1453937 B1 EP 1453937B1 EP 02787711 A EP02787711 A EP 02787711A EP 02787711 A EP02787711 A EP 02787711A EP 1453937 B1 EP1453937 B1 EP 1453937B1
Authority
EP
European Patent Office
Prior art keywords
catalyst bed
liquid
hydrogen
bed
catalyst
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.)
Expired - Lifetime
Application number
EP02787711A
Other languages
German (de)
English (en)
Other versions
EP1453937A1 (fr
Inventor
Antonius Adrianus Maria Roovers
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
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Priority to EP02787711A priority Critical patent/EP1453937B1/fr
Publication of EP1453937A1 publication Critical patent/EP1453937A1/fr
Application granted granted Critical
Publication of EP1453937B1 publication Critical patent/EP1453937B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/002—Apparatus for fixed bed hydrotreatment processes
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00

Definitions

  • the present invention is concerned with a method for hydroprocessing a hydrocarbonaceous feedstock at elevated temperature and pressure to obtain products, in particular fuels and/or middle distillates, which can be obtained in rather high yields at relatively low hydrogen consumption.
  • Hydroprocessing is well known in the art and has been practiced for many years and is still one of the important refinery processes. Over the years, a variety of feedstocks, catalysts and process conditions have been described for hydroprocessing of which many have been put into practice. For instance, in hydrocracking it is customary to pass the feedstock to be hydrocracked together with a hydrogen-containing gas over a catalyst bed containing a fixed array of particles containing one or more metal compounds having an intrinsic capability for breaking carbon-carbon bonds as well as one or more metal compounds having an intrinsic capability of hydrogenating fragments present after the cracking operation has been performed.
  • hydrocracking in which a feedstock and a hydrogen-containing gas are passed through the catalyst bed in the same direction, normally from top to bottom to make use of the gravity force, is known as co-current hydroprocessing. It is the oldest commercially applied hydrocracking method which is still in operation.
  • EP 287 234 discloses a process for catalytic hydrodewaxing of a hydrocarbon feedstock. The process is operated in countercurrent mode in a multiphase catalytic reactor comprising at least one fixed porous bed of catalyst particles with a void volume of 0.3 to 0.5. In the process as disclosed in EP 287 234 , there is a concentration gradient of the liquid. Therefore, the flow regime in the process of EP 287 234 is such that there is plug flow.
  • a major constraint in countercurrent hydroprocessing is the risk that conventional fixed bed reactors are susceptible to a phenomenon normally referred to as "catalyst bed flooding" which will occur when the velocity of the upflowing hydrogen-containing gas is such that it prevents the downward gravitational flow of the feedstock to be hydroprocessed during its passage through the catalyst bed.
  • catalyst contacting might improve as the bed approaches a flooded condition, it also makes the process rather vulnerable towards fluctuations in pressure or temperature or in fluid flow rates. Should a disturbance occur which is capable of initiating flooding it would cause disruption of the process, even to the extent of an unscheduled shutdown in order to recover stable operation.
  • countercurrent hydroprocessing can be carried out in reaction zones having a lower void fraction and which do not require specific means for preventing flooding of the catalyst bed.
  • the countercurrent hydroprocessing method according to the present invention is preferably carried out under flooding conditions. It also allows a higher yield than is achievable in cocurrent hydroprocessing. It has also been found that the process in accordance with the present invention allows a lower consumption of expensive hydrogen, a higher heavy ends conversion and a higher selectivity in the sulphur removal of higher boiling sulphur containing components.
  • the present invention therefore relates to a method for the hydroprocessing of a heavy hydrocarbonaceous feedstock in a reaction zone comprising a bed containing a fixed array of porous catalyst particles by contacting the feedstock with a hydrogen-containing gas under conditions which allow distributing the feedstock predominantly in liquid phase under superatmospheric process conditions at elevated temperature over the catalyst bed for downward flow in contact with the catalyst particles and introduction of the hydrogen-containing gas in the reaction zone below the catalyst bed in order to establish countercurrent contact of the upwardly flowing gas with the downcoming liquid and withdrawing treated liquid below the catalyst bed and withdrawing fluid depleted in hydrogen above the catalyst bed, in which process the catalyst bed has a void volume fraction below 0.5, whilst the countercurrent liquid/gas contacting is carried out under conditions which allow the Peclet number of the liquid to be in the range between 0 and 10.
  • Parameters which can be instrumental in providing countercurrent liquid/gas contacting comprise, inter alia, the gas rate (an increased gas rate reducing the unwanted static hold up), the liquid flow and the size of the restrictions in the introduction means for the gas. Those skilled in the art will know how to apply one or more of such parameters to allow for the appropriate Peclet number to be reached in the countercurrent hydroprocessing method according to the present invention.
  • the void volume fraction of a catalyst bed is defined for the purposes of this invention as 'one minus the fraction of the volume occupied by the catalyst particles of the total volume of the reaction zone'. It will be clear that the internal pore volume of the solid catalyst particles is not included in the definition of the void volume fraction which is built up of the interstitial voids between the catalyst particles and between the appropriate catalyst particles and the walls of the reaction zone in which they are contained.
  • void volume fractions of catalyst beds above 0.25 can be used in the method according to the present invention.
  • Preferred values are in the range between 0.30 and 0.48, especially preferred values are in the range between 0.35 and 0.47. Impressive results have been obtained using catalyst particles which have been packed in such a way that the void volume fraction is 0.45 (whilst operating under conditions allowing for the Peclet number of the liquid to be between 0 and 10).
  • the Peclet number for systems in which liquids and gases come into contact with each other whilst the solid phase is fixed can be defined as the ratio between the transport rate by convection and the transport rate by dispersion; Chemical Reactor Design and Operation. K. Westerterp et. al. ISBN 0 471 90183 0 .
  • the Peclet number for a totally back-mixed system (normally occurring when operating under CSTR conditions - CSTR meaning Continuously Stirred Tank Reactor) is defined as 0 whilst the Peclet number of a system operating in plug flow (e.g. in conventional trickle flow hydrocracking) in which by definition backflow is absent is defined as infinite ( ⁇ ).
  • the preferred range for the Peclet number of the liquid in the method of the present invention is between 1 and 8. It will be clear to those skilled in the art how to calculate the actual Peclet number for a given situation. As stated hereinbefore, it is the combination of the use of a catalyst bed having a low void fraction under conditions which allow a low Peclet number of the liquid which allow for the improved performance of the hydroprocessing method according to the present invention.
  • the catalysts to be used in the hydroprocessing method according to the present invention are well known in the art. They normally contain one or more metal(s) of Group VI and/or one or more non-noble metal(s) of Group VIII of the Periodic Table of the Elements which are conveniently present as oxides and/or as sulphides. Suitable Group VI elements are molybdenum and tungsten; suitable Group VIII metals are nickel and cobalt. The amounts of the metal compound(s) to be used can vary between wide ranges. Suitable ranges are between 2 and 40% by weight of Group VI metal compounds, expressed as metal, and between 1 and 10% by weight of Group VIII metal compounds, expressed as metal.
  • the catalyst particles will have the catalytically active metals present on a carrier.
  • Suitable carrier materials are inorganic refractory oxides such as alumina, silica, silica-alumina. magnesia, titania, zirconia and mixtures of two or more of such materials.
  • the catalyst particles may (additionally) contain dedicated cracking components such as zeolites and/or amorphous silica-alumina. Examples of suitable cracking components are well known in the art.
  • Suitable zeolites comprise zeolite Y and zeolite ⁇ but also non-zeolitic components can be used such as (silico)-alumino phosphates and related compounds.
  • a wide variety of catalyst shapes can be used in the method of hydroprocessing according to the present invention, such as spherical particles, cylindrical particles and polylobal particles such as trilobes and quadrulobes. Good results have been obtained using trilobal catalyst particles. Particles having a largest diameter between 0.5 and 3.5 mm are preferably applied. Good results have been obtained using trilobal catalyst particles having a diameter of 1.6 mm.
  • the hydroprocessing method according to the present invention can be conveniently carried out using a temperature in the range between 200 °C and 475 °C, preferably in the range between 250 °C and 425 °C and at a pressure between 20 and 250 bar, preferably between 40 and 160 bar.
  • the process can be carried out at a LHSV in the range between 1 and 20 Nl feed/l catalyst/hr and at a hydrogen/hydrocarbon feed ratio in the range between 100 and 2000 N1/1, preferably between 250 and 1500 N1/1. It will be clear that the set of process conditions has to be chosen in such a way that it allows the Peclet number of the liquid to be in the range between 0 and 10 (the void volume fraction of the catalyst bed in the reaction zone being less than 0.5 as discussed hereinbefore).
  • Heavy hydrocarbonaceous feedstocks to be used in the method according to the present invention comprise the usual feedstocks which are commercially used in hydrocracking such as heavy gas oils and the like. Suitable feedstocks have an initial boiling point of at least 200 °C whilst feedstocks containing substantial amounts of material boiling above 520 °C, e.g. containing up to 40% by weight of such material, can also be processed satisfactorily.
  • Normal impurities comprise light hydrocarbons and nitrogen.
  • Liquid feedstock is introduced via line 1 at the top of reaction zone 10 containing catalyst bed 11 and is distributed (means not shown) over the catalyst bed whilst a hydrogen-containing gas is introduced via line 2 below catalyst bed 11 in reaction zone 10 and rises up through the catalyst bed.
  • Treated liquid is withdrawn from reaction zone 10 via line 3 and can be used as such or may be subjected to further processing/upgrading (not shown) and fluid depleted in hydrogen is withdrawn from reaction zone 10 via line 4 which can be cooled down in order to separate off liquid present therein (means not shown).
  • the process as described in Figure 1 is carried out under conditions which allow a low Peclet number for the liquid in catalyst bed 11.
  • the line-up as described in Figure 2B is that as described in Figure 2A with the addition of a further reaction zone 30 containing catalyst bed 31 above reaction zone 10 containing catalyst bed 11.
  • Catalyst bed 31 is operated in trickle flow mode (high Peclet number of the liquid) and fluid depleted in hydrogen is withdrawn via line 7 which can be cooled down in order to separate off liquid present therein (means not shown).
  • liquid feedstock can be introduced additionally via line 8 on top of catalyst bed 31 in reaction zone 30.
  • Liquid feedstock is introduced via line 1 at the top of reaction zone 10 containing catalyst bed 11 and is distributed (means not shown) over the catalyst bed whilst a hydrogen-containing gas is introduced via line 2 below catalyst bed 11 in reaction zone 10 and rises up through catalyst bed 11.
  • Treated liquid is withdrawn from reaction zone 10 and sent (at least partially) via line 3 to be combined with fluid depleted in hydrogen which has been (at least partially) withdrawn from reaction zone 10 via line 4. It is, of course, possible and preferred in practice, to allow part of the fluid exiting reaction zone 10 via line 4 to be condensed so that a gas/liquid mixture will be combined with treated fluid ex line 3 to form feedstock entering reaction zone 40 via line 13.
  • the mixture is thus sent via line 13 to reaction zone 40 containing catalyst bed 41 which is operated (as hydroprocessing unit) in trickle flow mode (high Peclet number of the liquid).
  • the hydrogen required for this part of the process can be supplied via line 14 at the top of reaction zone 40, thereby allowing for cocurrent hydroprocessing of the mixture entering reaction zone 40 via line 13, or via line 14 at the bottom of reaction zone 40 thereby causing the catalyst bed 41 to be operated in countercurrent mode.
  • Treated liquid is withdrawn via line 15 and fluid depleted in hydrogen is withdrawn via line 16.
  • a heavy gas oil was led downwardly through the catalyst bed and hydrogen was led via the bottom part of the catalyst bed in countercurrent to the heavy gas oil.
  • the catalyst bed was loaded in such a way that the void fraction was 0.45.
  • the Initial Boiling Point (IBP) of the gas oil was 230 °C; 62% boiled above 340 °C and its Final Boiling Point (FBP) was 450 °C. It contained 2.1 %wt of sulphur and 317 ppm of nitrogen.
  • the conditions as pertaining in experiment 2 can be described as flooded countercurrent yielding a Peclet number of the liquid of 6 (calculated using the Westerterp reference referred to hereinabove).

Claims (10)

  1. Procédé pour l'hydrotraitement d'une charge d'alimentation hydrocarbonée lourde dans une zone de réaction comprenant un lit contenant un agencement fixe de particules de catalyseur poreuses par la mise en contact de la charge d'alimentation avec un gaz contenant de l'hydrogène sous des conditions qui permettent une distribution de la charge d'alimentation essentiellement en phase liquide sous des conditions de traitement superatmosphériques à température élevée sur le lit de catalyseur pour un écoulement descendant au contact des particules de catalyseur et l'introduction du gaz contenant de l'hydrogène dans la zone de réaction en dessous du lit de catalyseur afin d'établir un contact à contre-courant du gaz montant avec le liquide descendant ainsi que le prélèvement du liquide traité en dessous du lit de catalyseur et le prélèvement du fluide épuisé en hydrogène au-dessus du lit de catalyseur, procédé dans lequel le lit de catalyseur a une fraction de volume des vides en dessous de 0,5, alors que la mise en contact liquide/gaz à contre-courant est réalisée sous des conditions qui permettent au nombre de Peclet du liquide de se situer dans la plage entre 0 et 10.
  2. Procédé suivant la revendication 1, dans lequel le lit de catalyseur a une fraction de volume des vides au-dessus de 0,25.
  3. Procédé suivant la revendication 2, dans lequel le lit de catalyseur a une fraction de volume des vides entre 0,30 et 0,48, avantageusement entre 0,35 et 0,47
  4. Procédé suivant l'une quelconque des revendications précédentes, dans lequel la mise en contact à contre-courant est réalisée sous des conditions qui permettent au nombre de Peclet du liquide de se situer dans la plage entre 1 et 8.
  5. Procédé suivant l'une quelconque des revendications précédentes, dans lequel le liquide traité qui a été entraîné vers le bas dans le lit de catalyseur est amené en mode d'écoulement ruisselant dans un autre lit contenant des particules catalytiques avant son prélèvement du procédé.
  6. Procédé suivant l'une quelconque des revendications précédentes, dans lequel le fluide épuisé en hydrogène que l'on a fait monter dans le lit de catalyseur est entraîné vers le haut en phase vapeur dans un autre lit contenant des particules catalytiques avant son prélèvement du procédé comme fluide épuisé en hydrogène.
  7. Procédé suivant la revendication 6, dans lequel au moins une partie du gaz contenant de l'hydrogène montant est introduite dans le bas de la zone de réaction contenant un autre lit contenant des particules catalytiques dans lequel on fait passer le liquide traité avant son prélèvement du procédé.
  8. Procédé suivant l'une quelconque des revendications 1 à 6, dans lequel au moins une partie du liquide traité et au moins une partie du fluide épuisé en hydrogène sont combinées et soumises à une seconde étape d'hydrotraitement qui est réalisée de façon cocourante ou à contre-courant.
  9. Procédé suivant l'une quelconque des revendications précédentes, dans lequel l'hydrotraitement est réalisé sous des conditions d'hydrocraquage, notamment à une température se situant entre 200°C et 475°C et à une pression entre 20 et 250 bars.
  10. Procédé suivant la revendication 9, dans lequel on utilise des particules de catalyseur ayant une forme sphérique, cylindrique ou polylobée et un plus grand diamètre entre 0,5 et 3,5 mm.
EP02787711A 2001-11-16 2002-11-15 Hydrocraquage a contre courant Expired - Lifetime EP1453937B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP02787711A EP1453937B1 (fr) 2001-11-16 2002-11-15 Hydrocraquage a contre courant

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
EP01309668 2001-11-16
EP01309668 2001-11-16
EP02787711A EP1453937B1 (fr) 2001-11-16 2002-11-15 Hydrocraquage a contre courant
PCT/EP2002/012856 WO2003042333A1 (fr) 2001-11-16 2002-11-15 Hydrocraquage a contre courant

Publications (2)

Publication Number Publication Date
EP1453937A1 EP1453937A1 (fr) 2004-09-08
EP1453937B1 true EP1453937B1 (fr) 2007-08-01

Family

ID=8182463

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02787711A Expired - Lifetime EP1453937B1 (fr) 2001-11-16 2002-11-15 Hydrocraquage a contre courant

Country Status (15)

Country Link
US (1) US20050000858A1 (fr)
EP (1) EP1453937B1 (fr)
JP (1) JP2005509083A (fr)
KR (1) KR20050044435A (fr)
CN (1) CN1309808C (fr)
AT (1) ATE368718T1 (fr)
AU (1) AU2002352037B2 (fr)
BR (1) BR0214086A (fr)
CA (1) CA2467094A1 (fr)
DE (1) DE60221564T2 (fr)
MX (1) MXPA04004652A (fr)
NO (1) NO20042496L (fr)
RU (1) RU2288253C2 (fr)
WO (1) WO2003042333A1 (fr)
ZA (1) ZA200403161B (fr)

Families Citing this family (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7435336B2 (en) * 2002-10-10 2008-10-14 China Petroleum & Chenical Corporation Process for carrying out gas-liquid countercurrent processing
US7879223B2 (en) 2003-12-19 2011-02-01 Shell Oil Company Systems and methods of producing a crude product
EP2526898B1 (fr) * 2003-12-23 2013-04-17 Sadra Medical, Inc. Valvule cardiaque repositionnable
US20050137694A1 (en) 2003-12-23 2005-06-23 Haug Ulrich R. Methods and apparatus for endovascularly replacing a patient's heart valve
US7354507B2 (en) 2004-03-17 2008-04-08 Conocophillips Company Hydroprocessing methods and apparatus for use in the preparation of liquid hydrocarbons
DE102005003632A1 (de) 2005-01-20 2006-08-17 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Katheter für die transvaskuläre Implantation von Herzklappenprothesen
US7422904B2 (en) 2005-02-04 2008-09-09 Exxonmobil Chemical Patents Inc. Method of operating a fixed bed reactor under predetermined hydraulic conditions
US7896915B2 (en) 2007-04-13 2011-03-01 Jenavalve Technology, Inc. Medical device for treating a heart valve insufficiency
US9044318B2 (en) 2008-02-26 2015-06-02 Jenavalve Technology Gmbh Stent for the positioning and anchoring of a valvular prosthesis
ES2903231T3 (es) 2008-02-26 2022-03-31 Jenavalve Tech Inc Stent para el posicionamiento y anclaje de una prótesis valvular en un sitio de implantación en el corazón de un paciente
US8313705B2 (en) * 2008-06-23 2012-11-20 Uop Llc System and process for reacting a petroleum fraction
CN103002833B (zh) 2010-05-25 2016-05-11 耶拿阀门科技公司 人工心脏瓣及包括人工心脏瓣和支架的经导管输送的内假体
US9365781B2 (en) 2012-05-25 2016-06-14 E I Du Pont De Nemours And Company Process for direct hydrogen injection in liquid full hydroprocessing reactors
US9867694B2 (en) 2013-08-30 2018-01-16 Jenavalve Technology Inc. Radially collapsible frame for a prosthetic valve and method for manufacturing such a frame
CN107530168B (zh) 2015-05-01 2020-06-09 耶拿阀门科技股份有限公司 在心脏瓣膜替换中具有降低的起搏器比例的装置和方法
WO2017195125A1 (fr) 2016-05-13 2017-11-16 Jenavalve Technology, Inc. Système d'implantation de prothèse de valve cardiaque et procédé pour la pose d'une prothèse de valve cardiaque avec une gaine d'introduction et système de chargement
CN110392557A (zh) 2017-01-27 2019-10-29 耶拿阀门科技股份有限公司 心脏瓣膜模拟
CN113198624B (zh) * 2021-05-08 2022-03-01 华东理工大学 两相流体强传质逆流接触的方法和装置

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0287234A1 (fr) * 1987-04-14 1988-10-19 Mobil Oil Corporation Procédé d'hydrodéparaffinage multiphasique à contre-courant
US5578197A (en) * 1989-05-09 1996-11-26 Alberta Oil Sands Technology & Research Authority Hydrocracking process involving colloidal catalyst formed in situ
RU2128681C1 (ru) * 1993-10-08 1999-04-10 Акцо Нобель Н.В. Способ превращения парафинсодержащего углеводородного сырья
US5985135A (en) * 1998-10-23 1999-11-16 Exxon Research And Engineering Co. Staged upflow and downflow hydroprocessing with noncatalytic removal of upflow stage vapor impurities
FR2806642B1 (fr) * 2000-03-27 2002-08-23 Inst Francais Du Petrole Procede de conversion d'hydrocarbures dans un reacteur triphasique

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

Also Published As

Publication number Publication date
US20050000858A1 (en) 2005-01-06
DE60221564D1 (de) 2007-09-13
CN1309808C (zh) 2007-04-11
ATE368718T1 (de) 2007-08-15
RU2004118073A (ru) 2006-01-10
DE60221564T2 (de) 2008-04-17
BR0214086A (pt) 2004-09-28
AU2002352037B2 (en) 2007-05-17
ZA200403161B (en) 2005-01-14
RU2288253C2 (ru) 2006-11-27
MXPA04004652A (es) 2004-08-13
EP1453937A1 (fr) 2004-09-08
CA2467094A1 (fr) 2003-05-22
JP2005509083A (ja) 2005-04-07
WO2003042333A1 (fr) 2003-05-22
KR20050044435A (ko) 2005-05-12
NO20042496L (no) 2004-06-15
CN1589310A (zh) 2005-03-02

Similar Documents

Publication Publication Date Title
EP1453937B1 (fr) Hydrocraquage a contre courant
JP4074667B2 (ja) 単一反応槽における多段水素処理方法
US8926824B2 (en) Process for the conversion of residue integrating moving-bed technology and ebullating-bed technology
JP4150432B2 (ja) 向流反応器
AU2002352037A1 (en) Countercurrent hydroprocessing
US7507325B2 (en) Process for converting heavy petroleum fractions for producing a catalytic cracking feedstock and middle distillates with a low sulfur content
EP0944692B1 (fr) Hydrocraquage dans une cuve a reaction a contre courant
EP2782977B1 (fr) Procedé et systeme d'hydrocracquage en suspension
EP0272038B1 (fr) Procédé d'hydrocraquage d'huiles lourdes
US20030089638A1 (en) Process for converting heavy petroleum fractions including an ebulliated bed for producing middle distillates with a low sulfur content
WO1998007490A1 (fr) Cuve a reaction a contre courant
CN113383057B (zh) 包括在第二加氢裂化步骤下游进行的氢化步骤的生产石脑油的两步加氢裂化方法
EP0354626B1 (fr) Procédé d'hydrocraquage de charges hydrocarbonées
CN100381543C (zh) 一种复合催化剂床层的加氢裂化方法
EP0354623B1 (fr) Procédé d'hydrocraquage de charges hydrocarbonées
JP2761435B2 (ja) 向流移動触媒床中でのガス含有供給物の炭化水素処理
CN113557289A (zh) 用于生产中间馏分油的包括第二氢化裂解步骤下游的氢化步骤的两步氢化裂解方法
CN112342058A (zh) 一种催化裂化油浆的处理方法及其系统
JP2002322484A (ja) 水素添加方法
US11084991B2 (en) Two-phase moving bed reactor utilizing hydrogen-enriched feed
US3457161A (en) Process for treatment of mineral oils
CN115124401A (zh) 一种多产低碳烯烃的方法及系统
WO1994022982A1 (fr) Procede d'hydrocraquage/hydrotraitement integre

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

17P Request for examination filed

Effective date: 20040427

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LI LU MC NL PT SE SK TR

AX Request for extension of the european patent

Extension state: AL LT LV MK RO SI

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LI LU MC NL PT SE SK TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

REF Corresponds to:

Ref document number: 60221564

Country of ref document: DE

Date of ref document: 20070913

Kind code of ref document: P

ET Fr: translation filed
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20071101

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20071112

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

Ref country code: CH

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

Ref country code: AT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20071102

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20080102

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

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

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20071130

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20071101

26N No opposition filed

Effective date: 20080506

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20071115

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

Ref country code: FR

Payment date: 20080919

Year of fee payment: 7

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

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

Ref country code: DE

Payment date: 20081127

Year of fee payment: 7

Ref country code: NL

Payment date: 20081127

Year of fee payment: 7

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

Ref country code: GB

Payment date: 20081022

Year of fee payment: 7

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20071115

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20070801

REG Reference to a national code

Ref country code: NL

Ref legal event code: V1

Effective date: 20100601

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20091115

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20100730

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20100601

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20091130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20100601

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20091115

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20071130