EP0323297A1 - Wirbelschichtverfahren zur Kohlenwasserstoffumwandlung - Google Patents

Wirbelschichtverfahren zur Kohlenwasserstoffumwandlung Download PDF

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Publication number
EP0323297A1
EP0323297A1 EP88403153A EP88403153A EP0323297A1 EP 0323297 A1 EP0323297 A1 EP 0323297A1 EP 88403153 A EP88403153 A EP 88403153A EP 88403153 A EP88403153 A EP 88403153A EP 0323297 A1 EP0323297 A1 EP 0323297A1
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EP
European Patent Office
Prior art keywords
hydrocarbons
temperature
reaction zone
catalyst
particles
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Granted
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EP88403153A
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English (en)
French (fr)
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EP0323297B1 (de
Inventor
Jean-Louis Mauleon
Jean-Bernard Sigaud
Jean-Claude Courcelle
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TotalEnergies Marketing Services SA
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Total France SA
Compagnie de Raffinage et de Distribution Total France SA
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    • 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 and device 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 atoms of carbon, 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 increasing 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, naphthas, or finally sometimes diesel). 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.
  • a catalytic cracking unit in a conventional fluidized bed in English Fluid Catalytic Cracking, or FCC process
  • the hydrocarbon charge generally composed of gas oils or heavier charges such as distillation
  • a cracking catalyst which is kept in suspension in the vapors of the feed.
  • the catalyst is separated from the products obtained, stripped, regenerated by combustion of the coke formed, then brought back into contact with the charge to crack.
  • This catalytic cracking reaction takes place in a temperature range generally between 450 and 550 ° C. It is implemented so that the cracking unit is in thermal equilibrium without using energy annexed to the heating.
  • the supply of hot catalyst regenerated by combustion of the coke deposited during the reaction must be such that it can meet the various thermal requirements of the reaction section, namely, in particular: - preheating of the liquid charge, - the vaporization of this charge, - the calorie intake required by the reactions involved, which are generally endothermic.
  • the present invention relates to a method and a device for carrying out, in the same reaction zone, in dilute fluidized phase, of essentially ascending or descending type, on the one hand, a thermal cracking reaction with water vapor of light hydrocarbon feedstocks, which may include saturated light gases or cuts ranging from gasolines to diesel fuels, and, on the other hand, a catalytic cracking reaction of heavy hydrocarbon feedstocks, including a substantial part of the range d boiling is 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 .
  • the present invention therefore relates to a process for converting petroleum hydrocarbons, in the presence of catalyst particles in the fluidized phase, in a tubular reaction zone with essentially ascending or descending flow, this process comprising at least one step of steam cracking of at least one cut of light hydrocarbons, in the upstream part of the reaction zone, and a catalytic cracking step of at least one cut of heavy hydrocarbons, in the downstream part of said reaction zone, a step of ballistic separation of the spent catalyst particles, a step of regenerating this catalyst in at least one zone for burning the coke deposited on these particles and a step of recycling the regenerated particles to the supply of the reaction zone, this process being characterized in what: the steam cracking is carried out by bringing into contact, in a fluidized bed, the particles of catalyst, said light hydrocarbons and an amount of water vapor equal to at least 20% by weight and preferably between 30 and 50% by weight of the quantity of light hydrocarbons, the temperature resulting from said contacting being between 650 and 850 ° C and
  • 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 is reflected, 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 the European patent No. 208.609), with the consequence of a significant improvement in the yield of petrol and diesel compared to the quantity 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.
  • the production of propylene can also be significantly increased by judicious reuse of the hydrocarbons with two carbon atoms produced during the reaction.
  • the mixture of ethylene ethane coming from the fractionation zone of a type known per se, and to send this mixture to a trimerization or oligomerization reactor of the ethylene, for example of the type described by the prior art (for this purpose refer to European patents 12 685, 24 971, 215 609 or to American patent 4 605 807), to recover, after fractionation of the effluents: -
  • the unreacted ethane which will be recycled at the inlet of the upstream part of the reaction zone, in accordance with the present invention.
  • 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 can be diluted or not by conventional lighter cuts, can include cuts of hydrocarbons having 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 present invention therefore also relates to a device for converting fluidized catalytic phases of petroleum fractions, this device comprising a reaction zone for bringing petroleum fractions at high temperature into contact with catalyst particles in a tubular type reactor with essentially flow ascending or descending, 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 particles cells regenerated at the supply to said reactor, said device being characterized in that it comprises means for injecting at least one section of light hydrocarbons such as saturated light gases, gasolines or gas oils in the upstream part of the tubular reactor in the presence of water vapor in an amount equal to at least 20% by weight and, preferably, comprised e between 30 and 50% by weight relative to the amount of hydrocarbons, so that the resulting mixture is kept at a temperature between 650 and 850 ° C in a diluted fluidized bed, and in that it comprises in the downstream part of the tubular reactor first means for spraying at least
  • 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 microns.
  • 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.
  • reaction effluents leaving the stripping zone via line 16 are sent to a fractionation device schematically represented at 35, making it possible to separate: - by line 36, light gases or dry gases, (composed in particular of hydrogen, methane, ethane, ethylene, C3 to C5 hydrocarbons of NH3 and H2S), which can be then treated in another fractionation device 37, making it possible, in a manner known per se, to separate ethane and ethyl via line 38 and the C3 to C5 hydrocarbons which exit through line 39; - via line 40, the gasoline section, the boiling range of which generally extends from section C5 to around 160-220 ° C; - by line 41, the diesel cut, often also called LCO, whose boiling range generally extends from 160-220 ° C (start of cut) until around 320-380 ° C (end of cut); - via line 42, the heavy thinner cut, often also called HCO, which is less well valued (low viscosity fuel base) and whose
  • 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: Upstream riser area: Ethane injection - Regenerated catalyst temperature (° C) : 800 - Flow rate of regenerated catalyst (t / h) : 720 - Steam flow at 320 ° C (t / h) : 40 - Ethane flow (t / h) : 5 - Mixing temperature (° C) : 785 Fuel injection - Steam flow at 320 ° C (t / h) : 1 - Fuel flow at 150 ° C (t / h) : 20 - Mixing temperature (° C) : 725
  • Downstream riser area Charge injection - Steam flow at 320 ° C (t /

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  • 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 Wirbelschichtverfahren zur Kohlenwasserstoffumwandlung Expired - Lifetime EP0323297B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR8718375 1987-12-30
FR8718375A FR2625509B1 (fr) 1987-12-30 1987-12-30 Procede et dispositif de conversion d'hydrocarbures en lit fluidise
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 true EP0323297A1 (de) 1989-07-05
EP0323297B1 EP0323297B1 (de) 1991-06-19

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EP88403153A Expired - Lifetime EP0323297B1 (de) 1987-12-30 1988-12-12 Wirbelschichtverfahren zur Kohlenwasserstoffumwandlung

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

Cited By (14)

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Publication number Priority date Publication date Assignee Title
WO1991003527A1 (fr) * 1989-09-01 1991-03-21 Compagnie De Raffinage Et De Distribution Total France Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee
FR2655053A1 (fr) * 1989-11-24 1991-05-31 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.
FR2658833A1 (fr) * 1990-02-26 1991-08-30 Inst Francais Du Petrole Procede de craquage a l'etat fluide d'une charge d'hydrocarbures.
FR2659346A1 (fr) * 1990-03-09 1991-09-13 Inst Francais Du Petrole Procede de craquage avec oligomerisation ou trimerisation des olefines presentes dans les effluents.
EP0849347A2 (de) * 1996-12-17 1998-06-24 Exxon Research And Engineering Company Katalytische Krackverfahren für das wieder Kracken von katalytischem Naphta zur Erhöhung der Ausbeute von leichten Olefinen
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
WO1999055801A1 (en) * 1998-04-28 1999-11-04 Exxon Research And Engineering Company Fluid catalytic cracking process for converting a plurality of feeds
EP1046696A2 (de) * 1999-04-23 2000-10-25 China Petrochemical Corporation Verfahren zur katalytischen Umwandlung zum Herstellen von mit Isobutan und Isoparaffinen angereichertem Benzin
US6447671B1 (en) 1999-03-25 2002-09-10 Institut Francais Du Petrole Process for converting heavy petroleum fractions, comprising an ebullated bed hydroconversion step and a hydrotreatment step
WO2006071771A1 (en) * 2004-12-23 2006-07-06 Abb Lummus Global Inc. Processing of different feeds in a fluid catalytis cracking unit
EP1970427A2 (de) 2007-03-12 2008-09-17 Ivanhoe Energy, Inc. Verfahren und Systeme zur Herstellung von verringerten Rückständen und bodenlosen Produkten für schwere Kohlenwasserstoffeinsätze
WO2013083883A1 (fr) 2011-12-07 2013-06-13 IFP Energies Nouvelles Procede d'hydroconversion de charges petrolieres en lits fixes pour la production de fiouls a basse teneur en soufre
WO2014096703A1 (fr) 2012-12-20 2014-06-26 IFP Energies Nouvelles Procédé integré de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre
WO2014096704A1 (fr) 2012-12-20 2014-06-26 IFP Energies Nouvelles Procédé avec separation de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre

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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
WO2001000750A1 (en) * 1999-06-23 2001-01-04 China Petrochemical Corporation Catalytic converting process for producing prolifically diesel oil and liquefied gas
US7029571B1 (en) * 2000-02-16 2006-04-18 Indian Oil Corporation Limited Multi stage selective catalytic cracking process and a system for producing high yield of middle distillate products from heavy hydrocarbon feedstocks
DE60101338T2 (de) * 2000-07-12 2004-09-09 Shell Internationale Research Maatschappij B.V. Standrohreinlass zur verbesserung der zirkulation von partikelförmigen feststoffen für petrochemische oder andere verfahren
KR100939503B1 (ko) 2002-04-26 2010-01-29 차이나 페트로리움 앤드 케미컬 코포레이션 하향류 접촉분해 반응기 및 이의 용도
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
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
US8658023B2 (en) * 2010-12-29 2014-02-25 Equistar Chemicals, Lp Process for cracking heavy hydrocarbon feed
FR2981659B1 (fr) 2011-10-20 2013-11-01 Ifp Energies Now Procede 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
AU2012369895B2 (en) * 2012-02-14 2015-11-12 Reliance Industries Ltd. A process for catalytic conversion of low value hydrocarbon streams to light olefins
MY173254A (en) * 2012-08-09 2020-01-09 Linde Ag Method for preparing olefins by thermal steam-cracking
FR2999600B1 (fr) 2012-12-18 2015-11-13 IFP Energies Nouvelles Procede de raffinage d'une charge hydrocarbonee lourde mettant en oeuvre un desasphaltage selectif
US9896627B2 (en) * 2015-10-14 2018-02-20 Saudi Arabian Oil Company Processes and systems for fluidized catalytic cracking
EP3945066B1 (de) * 2020-07-28 2024-10-30 TotalEnergies OneTech Verfahren zur durchführung einer dampfcrackreaktion in einem wirbelschichtreaktor

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4422925A (en) * 1981-12-28 1983-12-27 Texaco Inc. Catalytic cracking
US4432863A (en) * 1981-07-20 1984-02-21 Ashland Oil, Inc. Steam reforming of carbo-metallic oils
EP0171460A1 (de) * 1984-06-13 1986-02-19 Ashland Oil, Inc. Verfahren zur katalytischen Spaltung von Residualölen mit Trockengas als Auftriebgas in einem Steigrohrreaktor
EP0208609A1 (de) * 1985-07-10 1987-01-14 Total Raffinage Distribution S.A. Verfahren und Einrichtung für das katalytische Kracken von Kohlenwasserstoffen mit Kontrolle der Reaktionstemperatur

Patent Citations (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
EP0171460A1 (de) * 1984-06-13 1986-02-19 Ashland Oil, Inc. Verfahren zur katalytischen Spaltung von Residualölen mit Trockengas als Auftriebgas in einem Steigrohrreaktor
EP0208609A1 (de) * 1985-07-10 1987-01-14 Total Raffinage Distribution S.A. Verfahren und Einrichtung für das katalytische Kracken von Kohlenwasserstoffen mit Kontrolle der Reaktionstemperatur

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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
WO1991003527A1 (fr) * 1989-09-01 1991-03-21 Compagnie De Raffinage Et De Distribution Total France Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee
AU641367B2 (en) * 1989-09-01 1993-09-23 Total Raffinage Distribution S.A. Method and device for vapor-cracking of hydrocarbons in fluidized phase
FR2655053A1 (fr) * 1989-11-24 1991-05-31 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.
FR2658833A1 (fr) * 1990-02-26 1991-08-30 Inst Francais Du Petrole Procede de craquage a l'etat fluide d'une charge d'hydrocarbures.
FR2659346A1 (fr) * 1990-03-09 1991-09-13 Inst Francais Du Petrole Procede de craquage avec oligomerisation ou trimerisation des olefines presentes dans les effluents.
DE4107043B4 (de) * 1990-03-09 2005-10-20 Inst Francais Du Petrole Verfahren für das thermische oder katalytische Kracken eines Kohlenwasserstoff-Einsatzprodukts
EP0849347A2 (de) * 1996-12-17 1998-06-24 Exxon Research And Engineering Company Katalytische Krackverfahren für das wieder Kracken von katalytischem Naphta zur Erhöhung der Ausbeute von leichten Olefinen
EP0849347A3 (de) * 1996-12-17 1998-12-09 Exxon Research And Engineering Company Katalytische Krackverfahren für das wieder Kracken von katalytischem Naphta zur Erhöhung der Ausbeute von leichten Olefinen
WO1999055801A1 (en) * 1998-04-28 1999-11-04 Exxon Research And Engineering Company Fluid catalytic cracking process for converting a plurality of feeds
US6447671B1 (en) 1999-03-25 2002-09-10 Institut Francais Du Petrole Process for converting heavy petroleum fractions, comprising an ebullated bed hydroconversion step and a hydrotreatment step
EP1046696A2 (de) * 1999-04-23 2000-10-25 China Petrochemical Corporation Verfahren zur katalytischen Umwandlung zum Herstellen von mit Isobutan und Isoparaffinen angereichertem Benzin
EP1046696A3 (de) * 1999-04-23 2001-01-03 China Petrochemical Corporation Verfahren zur katalytischen Umwandlung zum Herstellen von mit Isobutan und Isoparaffinen angereichertem Benzin
JP2008525597A (ja) * 2004-12-23 2008-07-17 エービービー ルマス グローバル インコーポレイテッド 流動接触分解ユニットにおける異質流体の処理
WO2006071771A1 (en) * 2004-12-23 2006-07-06 Abb Lummus Global Inc. Processing of different feeds in a fluid catalytis cracking unit
US8986617B2 (en) 2004-12-23 2015-03-24 Lummus Technology Inc. Processing of different feeds in a fluid catalytic cracking unit
US7682501B2 (en) 2004-12-23 2010-03-23 Abb Lummus Global, Inc. Processing of different feeds in a fluid catalytic cracking unit
AU2005322126B2 (en) * 2004-12-23 2011-09-15 Abb Lummus Global Inc. Processing of different feeds in a fluid catalytis cracking unit
CN101087865B (zh) * 2004-12-23 2014-05-07 Abb拉默斯环球有限公司 流化床催化裂化单元中不同进料的处理
KR101145196B1 (ko) * 2004-12-23 2012-05-25 루머스 테크놀로지 인코포레이티드 유동성 촉매분해시설에서의 별개의 피드의 프로세싱
US8377287B2 (en) 2007-03-12 2013-02-19 Ivanhoe Energy, Inc. Methods and systems for producing reduced resid and bottomless products from heavy hydrocarbon feedstocks
EP1970427A3 (de) * 2007-03-12 2012-05-09 Ivanhoe Energy Inc. Verfahren und Systeme zur Herstellung von verringerten Rückständen und bodenlosen Produkten für schwere Kohlenwasserstoffeinsätze
US8808632B2 (en) 2007-03-12 2014-08-19 Ivanhoe Energy Inc. Methods and systems for producing reduced resid and bottomless products from hydrocarbon feedstocks
EP1970427A2 (de) 2007-03-12 2008-09-17 Ivanhoe Energy, Inc. Verfahren und Systeme zur Herstellung von verringerten Rückständen und bodenlosen Produkten für schwere Kohlenwasserstoffeinsätze
US9434888B2 (en) 2007-03-12 2016-09-06 Ivanhoe Htl Petroleum Ltd. Methods and systems for producing reduced resid and bottomless products from heavy hydrocarbon feedstocks
WO2013083883A1 (fr) 2011-12-07 2013-06-13 IFP Energies Nouvelles Procede d'hydroconversion de charges petrolieres en lits fixes pour la production de fiouls a basse teneur en soufre
WO2014096703A1 (fr) 2012-12-20 2014-06-26 IFP Energies Nouvelles Procédé integré de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre
WO2014096704A1 (fr) 2012-12-20 2014-06-26 IFP Energies Nouvelles Procédé avec separation de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre

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DE3863352D1 (de) 1991-07-25
CN1020344C (zh) 1993-04-21
ES2022682B3 (es) 1991-12-01
JPH01294794A (ja) 1989-11-28
FR2625509B1 (fr) 1990-06-22
EP0323297B1 (de) 1991-06-19
GR3002175T3 (en) 1992-12-30
JP2509314B2 (ja) 1996-06-19
CN1034949A (zh) 1989-08-23
ZA889689B (en) 1989-09-27
FR2625509A1 (fr) 1989-07-07

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