EP0323297B1 - Procédé de conversion d'hydrocarbures en lit fluidisé - Google Patents

Procédé de conversion d'hydrocarbures en lit fluidisé Download PDF

Info

Publication number
EP0323297B1
EP0323297B1 EP88403153A EP88403153A EP0323297B1 EP 0323297 B1 EP0323297 B1 EP 0323297B1 EP 88403153 A EP88403153 A EP 88403153A EP 88403153 A EP88403153 A EP 88403153A EP 0323297 B1 EP0323297 B1 EP 0323297B1
Authority
EP
European Patent Office
Prior art keywords
hydrocarbons
reaction zone
process according
catalyst
temperature
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
EP88403153A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0323297A1 (fr
Inventor
Jean-Louis Mauleon
Jean-Bernard Sigaud
Jean-Claude Courcelle
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.)
Total Marketing Services SA
Original Assignee
Compagnie de Raffinage et de Distribution Total France SA
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 Compagnie de Raffinage et de Distribution Total France SA filed Critical Compagnie de Raffinage et de Distribution Total France SA
Publication of EP0323297A1 publication Critical patent/EP0323297A1/fr
Application granted granted Critical
Publication of EP0323297B1 publication Critical patent/EP0323297B1/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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique

Definitions

  • the present invention relates to a conversion process allowing, in the same reaction zone, catalytic cracking from heavy hydrocarbon charges and the simultaneous production of olefins, in particular olefins comprising from 2 to 4 carbon atoms, by gentle steam cracking of light hydrocarbon charges.
  • hydrocarbon cracking processes are commonly used by the petroleum and oil services industries; they consist in dividing, by raising the temperature, hydrocarbon molecules into smaller molecules.
  • thermal cracking and catalytic cracking, which involve either the only influence of temperature or the active sites of a catalyst.
  • thermocracking reaction which is a globally endothermic reaction, takes place mainly in the part of the tubes receiving the maximum heat flux.
  • the temperature of these tubes is determined by the nature of the hydrocarbons to be cracked (they are generally either ethane or liquefied petroleum gases or LPG, or gasolines, or naphthas, or finally sometimes gas oils). Whatever the nature of the load, this temperature is always very high and greater than 700 ° C; it is however limited to a maximum of the order of 850 ° C. by the conditions of implementation of the method and by the complexity of operation of the ovens which use auxiliary heating energy.
  • the subject of the present invention is a process for carrying out, in the same reaction zone, in dilute fluidized phase, of ascending or descending type, on the one hand, a thermal cracking reaction with steam of hydrocarbon feedstocks light, which may include saturated light gases or cuts ranging from gasoline to diesel, and, on the other hand, a catalytic cracking reaction of heavy hydrocarbon charges, of which a substantial part of the boiling range is located above 500 ° C.
  • the present invention aims to use this feature of heavy loads to produce coke, not only to provide the catalyst, during the combustion of coke, the energy necessary for the vaporization of the heavy load, but also to provide energy to the catalyst. additional and thus create, in the upstream part of the reaction zone, the conditions required for carrying out a gentle steam cracking of lighter hydrocarbons, comprising in particular ethane, propane, butane, light gasolines, naphthas and gas oils .
  • Light hydrocarbons intended for steam cracking may be introduced into the reaction zone using one or more injection lines, depending on the nature of the hydrocarbons to be steam cracked.
  • the various cuts of hydrocarbons capable of being injected will be introduced one after the other from upstream to downstream in said reaction zone by Ascending of their boiling temperature, the lightest cup being introduced into the hottest area.
  • the steam cracking zone may be subdivided into as many zones, operating with decreasing severity, as there are sections of light saturated hydrocarbons intended for steam cracking.
  • the quantity of water vapor injected into the upstream part of the reaction zone is here significant compared to the usual cracking conditions in a fluidized bed. However, it remains appreciably lower than the values practiced in the conventional steam cracking process, in particular because the process described here accommodates without problem the possible formation of a certain amount of coke. Indeed, the amount of water vapor will usually be between 20 and 60% and, preferably, between 30 and 50% by weight, relative to the amount of hydrocarbons to be converted by steam cracking.
  • a first advantage of the process according to the invention is linked to the fact that the steam cracking reaction, in the upstream part of the reactor, requires significant amounts of calories due, essentially, to the very high endothermicity of this reaction (5 to 10 times higher than that of the catalytic cracking reaction).
  • This significant absorption of calories, in the upstream part of the reactor acts as a heat sink, which results, as in any catalytic cracking unit, by an increased flow rate of the catalyst circulation.
  • the catalytic cracking reaction will be carried out with a ratio of quantity of catalyst to quantity of filler to be cracked (generally called "C / O ratio") much higher than according to the prior art (see for this purpose EP-A -208.609), with the consequence of a significant improvement in the yield of gasoline and diesel compared to the amount of heavy load to be cracked.
  • this C / O ratio may advantageously be between 4 and 12 in the downstream part of the reaction zone.
  • a second advantage of the process according to the invention resides in the fact that it makes it possible to convert into ethylene, propylene and butenes, light cuts of low recovery, such as ethane or certain gasoline cuts, and this under selectivity conditions superior to conventional steam cracking.
  • the cracking unit will comprise a device for fractionating the reaction effluents making it possible to selectively fractionate, in a manner known per se, the abovementioned hydrocarbons as well as light gases and hydrocarbons with two, three or four carbon atoms.
  • the gentle steam cracking will be carried out in the upstream part of the reactor in at least two zones of decreasing severity, by injection in the presence of water vapor of at least two separate cuts: a cut containing mainly ethane, but also possibly propane and butane, then a cut containing light essences, then possibly naphtas or gas oils.
  • An additional advantage arising from the present invention resides in the fact that the hydrogen necessarily produced by steam cracking in the upstream part of the reactor is capable of reacting under the reaction conditions of the downstream part of the reactor and, therefore, of improving the yield effluents from the conversion unit into the best valued products.
  • the steam cracked hydrocarbon fractions usable according to the present invention therefore comprise saturated light gases, such as ethane, propane or butanes, or heavier hydrocarbons, saturated or not, such as light gasolines, naphthas or gas oils, or even certain cuts with a higher boiling point but highly paraffinic, such as paraffins or slack wax.
  • saturated light gases such as ethane, propane or butanes
  • heavier hydrocarbons saturated or not, such as light gasolines, naphthas or gas oils, or even certain cuts with a higher boiling point but highly paraffinic, such as paraffins or slack wax.
  • These hydrocarbon fractions can come either from different refinery units, such as atmospheric distillation, visbreaking, hydrocracking, oil manufacturing or olefin oligomerization units, or effluents from the unit of conversion itself.
  • the main charge injected downstream of the mild steam cracking zone could be a standard charge of a catalytic cracking unit, but with the possibility, compared to the known precedents, of also using heavier charges.
  • These fillers may, if necessary, have received a preliminary treatment, such as, for example, a hydrotreatment. They may, in particular, contain fractions rich in asphaltenes and having a Conradson carbon content. equal to or greater than 10%.
  • These charges may or may not be diluted by conventional lighter cuts, which may include cuts of hydrocarbons which have already undergone a cracking operation and which are recycled, such as cracked gas oils, LCOs or HCOs Finally, these charges can be preheated in a temperature range generally between 100 and 400 ° C.
  • the injection of hydrocarbons into the downstream part of the reaction zone is carried out using high-performance sprayers, such as nozzle sprayers of the venturi type, so as to give the droplets of liquid the smallest possible diameter. , generally less than 100 microns and preferably less than 50 microns.
  • This fine spray allows the droplets formed to be vaporized almost instantaneously, when they are brought into contact with the catalyst flow at high temperature.
  • the temperature for mixing the charge with the catalyst particles may be as high as necessary to obtain complete vaporization of all the constituents of the charge, while remaining independent of the final catalytic cracking temperature of the zone located further downstream, thanks to the injection, downstream of the residual main charge, of another cut of hydrocarbons, such as a cut HCO or LCO liquid, the latter cut being injected at a temperature and in an amount such that the temperature prevailing in the rest of the reaction zone can be adjusted, so that the catalytic cracking is carried out under optimal conditions.
  • another cut of hydrocarbons such as a cut HCO or LCO liquid
  • the device will include means for regulating the feed rate of the recycle so that the final reaction temperature is maintained equal to a set value adapted to the load to be cracked, to the cracking conditions and to the type of market sought (for example, petrol market: final temperature 500-530 ° C, or diesel market: final temperature 480-510 ° C).
  • a set value adapted to the load to be cracked, to the cracking conditions and to the type of market sought (for example, petrol market: final temperature 500-530 ° C, or diesel market: final temperature 480-510 ° C).
  • the mixing temperature of the vaporized charge to be cracked and the catalyst can thus be maintained above the dew point of the charge, while adapting the cracking temperature to the selectivity desired for the cracking effluents.
  • the process according to the invention can advantageously be implemented in a device comprising a reaction zone for bringing petroleum fractions at high temperature into contact with catalyst particles in a tubular type reactor with essentially ascending or descending flow, means for ballistic separation of said particles and cracked cuts, means for stripping the catalyst particles, means for regenerating them by combustion of the coke deposited on these particles, and means for recycling the regenerated particles in the supply to said reactor ,
  • this device comprising means for injecting at least one section of light hydrocarbons such as saturated light gases, gasoline or diesel in the upstream part of the tubular reactor in the presence of water vapor in an amount equal to less than 20% by weight and preferably between 30 and 50% by weight relative to the quantity hydrocarbons, so that the resulting mixture is maintained at a temperature between 650 and 850 ° C in a dilute fluidised bed, said device further comprising in the downstream part of the tubular reactor first means for spraying at least one cut of heavier hydrocarbons under conditions such that the mixing temperature is higher than the vaporization temperature of said
  • This temperature of the conversion effluents will in particular be kept constant between 475 and 550 ° C. by spraying, downstream of the injection zone of the heavy load, with a determined quantity of LCO or HCO.
  • This spraying like that of the heavy load to be catalytically cracked, will be carried out using injectors of a type known per se, making it possible to obtain, at the outlet of the injector (s), droplets of which at least 80% have a diameter less than 100 micrometers.
  • the ratio between the flow rate of heavy hydrocarbon feed introduced into the downstream part and the flow of lighter hydrocarbons (in particular ethane and petrol) introduced into the upstream part can vary in significant proportions, for example in a ratio of between 0.20 and 1.50 by weight.
  • catalysts having catalytic cracking capacities can be used to carry out the process according to the present invention.
  • a particularly advantageous category is that of catalysts having porous structures in which molecules can be brought into contact with active sites located in the pores; in this class, there are in particular silicates or aluminosilicates.
  • catalysts containing zeolite are commercially available with supports containing a variety of metal oxides and combinations of said oxides, in particular silica, alumina, magnesia, oxides of titanium, barium, and mixtures of these substances, as well as mixtures of said oxides with clays, bridged or not.
  • the catalyst composition can naturally contain one or more agents promoting one or the other step of the process.
  • the catalyst may therefore, in particular, contain agents promoting the combustion of coke during regeneration.
  • the upward fluidized phase conversion device shown in this figure essentially comprises a column 1, called a load elevator, or riser. It is supplied at its base by line 2 with particles of regenerated catalyst particles, in a quantity regulated by a valve 3. The regenerated particles are fluidized by injection of steam or gas arriving by line 4 at the base of the riser , using a diffuser 5.
  • Light saturated gases comprising in particular ethane are then introduced into the column using the diffuser 7 supplied by line 6 with additional steam supplied by line 10.
  • a gasoline or diesel cut injected by a diffuser 8 supplied by the line 9, can in turn be cracked at a lower temperature level, of the order of 150 to 750 ° C.
  • a complement of steam can also be supplied by line 10 ′.
  • the load of hydrocarbons heavier than diesel is then introduced into the reactor using one or more injectors 11 supplied by line 12, in an amount such that the temperature prevailing in this part of column 1 is higher or equal to the vaporization temperature of said charge. It is then necessary to reduce the mixing temperature to a value more conducive to catalytic cracking, that is to say of the order of 475 to 550 ° C., by spraying with hydrocarbons such as light diluents (LCO) or heavy (HCO), using line 13 which supplies the injector (s) 14.
  • LCO light diluents
  • HCO heavy
  • Column 1 opens at its top into an enclosure 15, which is for example concentric with it and in which, on the one hand, the separation of the cracked charge takes place and, on the other hand, the stripping of the used particles.
  • the ballistic separation system cyclonic or not, is housed in the enclosure 15 and the effluent hydrocarbons are evacuated by an evacuation line 16, provided at the top of the enclosure 15, while the used catalytic particles descend to the base.
  • enclosure 15 where a line 17 supplies stripping gas (generally steam) to diffusers 18 regularly arranged at the base of this enclosure 15.
  • the particles thus stripped are evacuated towards the regenerator, via of a duct 19, on which a regulating valve 20 is provided.
  • the regenerator shown in this figure here comprises a first combustion zone 21, in the presence of oxygen, of the coke deposited on the catalyst particles.
  • the coke is thus mainly burnt using air, injected into the regenerator bar by a line 22, which feeds the diffuser 23.
  • the combustion gas is separated from the catalyst grains in the cyclone 24, whence the combustion gas is evacuated via a line 25, while the partially regenerated catalytic particles are transferred to the second stage 26 by the central duct 27, supplied with air by the line 28.
  • the base of the stage 26 can also be supplied with air by the diffuser 29, supplied by the line 30.
  • the grains of this regenerated catalyst are discharged laterally in a buffer enclosure 31 and recycled through line 2 to the supply to the elevator 1.
  • the combustion gases discharged at the upper part of the chamber 26 are treated in a cyclone 32, which is here external to the chamber and from the base of which the particles of the catalyst are returned via the conduit 33 into the chamber 26, while the combustion gases are evacuated via line 34.
  • the ethane and the ethylene coming from line 38 are introduced into an oligomerization reactor 44.
  • a fractionation device 45 then makes it possible to evacuate via line 46 unreacted ethane and ethylene, while light olefinic gasolines (whose boiling temperature is generally between 30 and 100 ° C) are extracted by line 47.
  • Line 46 then allows to return the ethane thus recovered in the upstream part of the reactor by line 6, while the light gasolines can either be recovered as such, or steam cracked by recycling in line 9, in order, for example, to maximize the production of propylene.
  • part of the HCO from the fractionation zone 35 is here recycled by line 42 to line 13 to regulate the reaction temperature downstream of column 1.
  • This regulation is done using a valve 48, the flow rate of which is for example adjusted as a function of the temperature measured using a probe preferably located at the outlet of the reactor.
  • valves 49 and 50 make it possible to regulate the quantities of light hydrocarbons introduced by lines 9 and 6 into the upstream part of the reaction zone, as a function of the temperature measured in this part, so that this temperature , between 650 and 850 ° C, allows to ensure steam cracking, in accordance with the present invention.
  • a commercial catalyst comprising ultra-stabilized zeolites and a matrix capable of cracking the heaviest hydrocarbon molecules.
  • the conditions of this test in which ethane and petrol are successively injected into the upstream part of the reaction zone, then successively the charge A and a determined quantity of HCO in the downstream part, are as follows:

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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP88403153A 1987-12-30 1988-12-12 Procédé de conversion d'hydrocarbures en lit fluidisé Expired - Lifetime EP0323297B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR8718375A FR2625509B1 (fr) 1987-12-30 1987-12-30 Procede et dispositif de conversion d'hydrocarbures en lit fluidise
FR8718375 1987-12-30
CN89100052A CN1020344C (zh) 1987-12-30 1988-12-30 流化床烃类转化方法和装置

Publications (2)

Publication Number Publication Date
EP0323297A1 EP0323297A1 (fr) 1989-07-05
EP0323297B1 true EP0323297B1 (fr) 1991-06-19

Family

ID=36699186

Family Applications (1)

Application Number Title Priority Date Filing Date
EP88403153A Expired - Lifetime EP0323297B1 (fr) 1987-12-30 1988-12-12 Procédé de conversion d'hydrocarbures en lit fluidisé

Country Status (8)

Country Link
EP (1) EP0323297B1 (ja)
JP (1) JP2509314B2 (ja)
CN (1) CN1020344C (ja)
DE (1) DE3863352D1 (ja)
ES (1) ES2022682B3 (ja)
FR (1) FR2625509B1 (ja)
GR (1) GR3002175T3 (ja)
ZA (1) ZA889689B (ja)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013057389A1 (fr) 2011-10-20 2013-04-25 IFP Energies Nouvelles Procédé de conversion de charges petrolieres comprenant une etape d'hydroconversion en lit bouillonnant et une etape d'hydrotraitement en lit fixe pour la production de fiouls a basse teneur en soufre
WO2014096602A1 (fr) 2012-12-18 2014-06-26 IFP Energies Nouvelles Procédé de raffinage d'une charge hydrocarbonée lourde mettant en oeuvre un des désasphaltage sélectif

Families Citing this family (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2786287B2 (ja) * 1989-09-01 1998-08-13 トータル、ラフィナージュ、ディストリビュシオン、ソシエテ、アノニム 流動相で炭化水素を蒸気クラッキングする方法および装置
AU641367B2 (en) * 1989-09-01 1993-09-23 Total Raffinage Distribution S.A. Method and device for vapor-cracking of hydrocarbons in fluidized phase
FR2655053B1 (fr) * 1989-11-24 1994-04-29 Inst Francais Du Petrole Procede et dispositif de regulation des conditions de fonctionnement d'un reacteur de craquage catalytique utilisant une source de rayonnements ionisants.
FR2658833B1 (fr) * 1990-02-26 1994-04-29 Inst Francais Du Petrole Procede de craquage a l'etat fluide d'une charge d'hydrocarbures.
FR2659346B1 (fr) * 1990-03-09 1994-04-29 Inst Francais Du Petrole Procede de craquage avec oligomerisation ou trimerisation des olefines presentes dans les effluents.
US5846403A (en) * 1996-12-17 1998-12-08 Exxon Research And Engineering Company Recracking of cat naphtha for maximizing light olefins yields
CN1056595C (zh) * 1997-10-20 2000-09-20 中国石油化工总公司 多种进料烃类直接转化制烯烃方法
JP2003517491A (ja) * 1998-04-28 2003-05-27 エクソンモービル リサーチ アンド エンジニアリング カンパニー 炭化水素混合物を転化するための改良流動接触分解プロセス
FR2791354B1 (fr) 1999-03-25 2003-06-13 Inst Francais Du Petrole Procede de conversion de fractions lourdes petrolieres comprenant une etape d'hydroconversion en lits bouillonnants et une etape d'hydrotraitement
EP1046696B1 (en) * 1999-04-23 2014-06-11 China Petrochemical Corporation A catalytic conversion process for producing isobutane and isoparaffin-enriched gasoline
JP4361234B2 (ja) * 1999-06-23 2009-11-11 中國石油化工集團公司 ディーゼル油の収率と液化ガスの収率を同時に増加させる接触分解法
CN100448953C (zh) * 2000-02-16 2009-01-07 印度石油股份有限公司 由重烃原料以高产率生产中间馏分产品的多级选择性催化裂化方法和系统
AU2001283939B2 (en) * 2000-07-12 2004-03-18 Shell Internationale Research Maatschappij B.V. Standpipe inlet for enhancing particulate solids circulation for petrochemical and other processes
WO2003090918A1 (fr) 2002-04-26 2003-11-06 China Petroleum & Chemical Corporation Reacteur de craquage catalytique a courant descendant
DE10260738A1 (de) 2002-12-23 2004-07-15 Outokumpu Oyj Verfahren und Anlage zur Förderung von feinkörnigen Feststoffen
JP2006063290A (ja) * 2004-08-30 2006-03-09 Ebara Corp 高分子炭化水素の利用システムおよび方法
US7682501B2 (en) * 2004-12-23 2010-03-23 Abb Lummus Global, Inc. Processing of different feeds in a fluid catalytic cracking unit
FR2894849B1 (fr) * 2005-12-20 2008-05-16 Inst Francais Du Petrole Nouveau reacteur a deux zones reactionnelles fluidisees avec systeme de separation gaz/solide integre
FR2895413B1 (fr) 2005-12-27 2011-07-29 Alstom Technology Ltd Installation de conversion d'hydrocarbures petroliers a installation de combustion integree comprenant une capture du dioxyde de carbone
CA2624746C (en) 2007-03-12 2015-02-24 Robert Graham Methods and systems for producing reduced resid and bottomless products from heavy hydrocarbon feedstocks
US8658023B2 (en) * 2010-12-29 2014-02-25 Equistar Chemicals, Lp Process for cracking heavy hydrocarbon feed
FR2983866B1 (fr) 2011-12-07 2015-01-16 Ifp Energies Now Procede d'hydroconversion de charges petrolieres en lits fixes pour la production de fiouls a basse teneur en soufre
AU2012369895B2 (en) * 2012-02-14 2015-11-12 Reliance Industries Ltd. A process for catalytic conversion of low value hydrocarbon streams to light olefins
IN2014DN11047A (ja) * 2012-08-09 2015-09-25 Linde Ag
FR3000098B1 (fr) 2012-12-20 2014-12-26 IFP Energies Nouvelles Procede avec separation de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre
FR3000097B1 (fr) 2012-12-20 2014-12-26 Ifp Energies Now Procede integre de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre
US9896627B2 (en) * 2015-10-14 2018-02-20 Saudi Arabian Oil Company Processes and systems for fluidized catalytic cracking
EP3945066A1 (en) * 2020-07-28 2022-02-02 Total Se Process to conduct a steam cracking reaction in a fluidized bed reactor

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4432863A (en) * 1981-07-20 1984-02-21 Ashland Oil, Inc. Steam reforming of carbo-metallic oils
US4422925A (en) * 1981-12-28 1983-12-27 Texaco Inc. Catalytic cracking
IN162877B (ja) * 1984-06-13 1988-07-16 Ashland Oil Inc
FR2584732B1 (fr) * 1985-07-10 1988-08-19 Raffinage Cie Francaise Procede et dispositif pour le craquage catalytique de charges d'hydrocarbures, avec controle de la temperature de reaction

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013057389A1 (fr) 2011-10-20 2013-04-25 IFP Energies Nouvelles Procédé de conversion de charges petrolieres comprenant une etape d'hydroconversion en lit bouillonnant et une etape d'hydrotraitement en lit fixe pour la production de fiouls a basse teneur en soufre
WO2014096602A1 (fr) 2012-12-18 2014-06-26 IFP Energies Nouvelles Procédé de raffinage d'une charge hydrocarbonée lourde mettant en oeuvre un des désasphaltage sélectif

Also Published As

Publication number Publication date
GR3002175T3 (en) 1992-12-30
CN1020344C (zh) 1993-04-21
DE3863352D1 (de) 1991-07-25
JP2509314B2 (ja) 1996-06-19
JPH01294794A (ja) 1989-11-28
FR2625509A1 (fr) 1989-07-07
ZA889689B (en) 1989-09-27
ES2022682B3 (es) 1991-12-01
EP0323297A1 (fr) 1989-07-05
CN1034949A (zh) 1989-08-23
FR2625509B1 (fr) 1990-06-22

Similar Documents

Publication Publication Date Title
EP0323297B1 (fr) Procédé de conversion d'hydrocarbures en lit fluidisé
EP0208609B1 (fr) Procédé et dispositif pour le craquage catalytique de charges d'hydrocarbures, avec contrôle de la température de réaction
US5264115A (en) Process and apparatus for fluidized bed hydrocarbon conversion
EP0191695B1 (fr) Procédé et dispositif d'injection de catalyseur dans un procédé de craquage catalytique à l'état fluide, notamment de charges lourdes
EP1656989B1 (fr) Dispositif et procédé pour le craquage catalytique de deux charges distinctes d'hydrocarbures
EP1170355B1 (fr) Procédé et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres réactionelles successives
EP0489726B1 (fr) Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee
FR2659346A1 (fr) Procede de craquage avec oligomerisation ou trimerisation des olefines presentes dans les effluents.
JPH06322377A (ja) 高および低コンカーボン成分を含むパラフィンリッチ供給原料を接触的にクラッキングする方法および装置
FR2654435A1 (fr) Procede et dispositif de mise en contact d'une charge d'hydrocarbures avec des particules solides chaudes, dans un reacteur tubulaire a lit fluidise ascendant.
JPH03197591A (ja) 炭化水素の接触分解方法
EP0874880B1 (fr) Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures
EP0291408B1 (fr) Procédé de vapocraquage dans une zone réactionnelle en lit fluide
EP0911379A1 (fr) Procédé et dispositif de vaporisation sélective des charges d'hydrocarbures en craquage catalytique
FR2682119A1 (fr) Perfectionnements aux dispositifs de craquage catalytique a l'etat fluide de charges d'hydrocarbures.
EP0265347A1 (fr) Procédé et dispositif pour le craquage catalytique en lit fluidisé d'une charge d'hydrocarbures
FR2658833A1 (fr) Procede de craquage a l'etat fluide d'une charge d'hydrocarbures.
WO1991003527A1 (fr) Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee
FR2628436A1 (fr) Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee de particules caloporteuses
FR2621322A1 (fr) Procede de vaporisation d'une charge liquide dans un procede de craquage catalytique en lit fluide
FR2617860A1 (fr) Procede de craquage a l'etat fluide d'une charge d'hydrocarbures
LU84039A1 (fr) Procede et appareil de vaporisation selective
FR2521157A1 (fr) Preparation d'une charge de craquage catalytique fluide par vaporisation selective
BE892090A (fr) Preparation d'une charge de craquage catalytique fluide par vaporisation selective
FR2523997A1 (fr) Procede et appareil de vaporisation selective pour l'elimination du carbone et des metaux contenus dans les fractions lourdes de petrole

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 GB GR IT LU NL

17P Request for examination filed

Effective date: 19890614

17Q First examination report despatched

Effective date: 19900706

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 GB GR IT LU NL

ITF It: translation for a ep patent filed

Owner name: BARZANO' E ZANARDO MILANO S.P.A.

REF Corresponds to:

Ref document number: 3863352

Country of ref document: DE

Date of ref document: 19910725

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)
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: 19911231

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

26N No opposition filed
REG Reference to a national code

Ref country code: GR

Ref legal event code: FG4A

Free format text: 3002175

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

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

Ref country code: NL

Payment date: 20071213

Year of fee payment: 20

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

Ref country code: IT

Payment date: 20071222

Year of fee payment: 20

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

Ref country code: BE

Payment date: 20071231

Year of fee payment: 20

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

Ref country code: ES

Payment date: 20071228

Year of fee payment: 20

Ref country code: GB

Payment date: 20071218

Year of fee payment: 20

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

Ref country code: GR

Payment date: 20071219

Year of fee payment: 20

Ref country code: DE

Payment date: 20071221

Year of fee payment: 20

BE20 Be: patent expired

Owner name: CIE DE RAFFINAGE ET DE DISTRIBUTION *TOTAL FRANCE

Effective date: 20081212

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Expiry date: 20081211

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 EXPIRATION OF PROTECTION

Effective date: 20081212

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20081213

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

Ref country code: ES

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20081213

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 EXPIRATION OF PROTECTION

Effective date: 20081211