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WO2009087576A2 - Procédé de craquage catalytique fluide employant des compositions de craquage basiques - Google Patents

Procédé de craquage catalytique fluide employant des compositions de craquage basiques Download PDF

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Publication number
WO2009087576A2
WO2009087576A2 PCT/IB2009/005002 IB2009005002W WO2009087576A2 WO 2009087576 A2 WO2009087576 A2 WO 2009087576A2 IB 2009005002 W IB2009005002 W IB 2009005002W WO 2009087576 A2 WO2009087576 A2 WO 2009087576A2
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Prior art keywords
basic material
catalyst
metal
group
pore zeolite
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WO2009087576A3 (fr
WO2009087576A9 (fr
Inventor
Elbert Arjan De Graaf
Leendert Arie Gerritsen
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Albemarle Netherlands BV
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Albemarle Netherlands BV
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Publication of WO2009087576A9 publication Critical patent/WO2009087576A9/fr
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • 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

  • Crude oil is a complex mixture of hydrocarbons.
  • crude oil is subjected to distillation processes to make a first separation by boiling point.
  • One of the main fractions obtained in this process is Vacuum Gas Oil (VGO), which is commonly treated further in a cracking process, in particular a fluid catalytic cracking (FCC) process.
  • VGO Vacuum Gas Oil
  • FCC fluid catalytic cracking
  • Other feedstocks for cracking process include among others hydrotreated VGO and atmospheric resid.
  • Cracking is the process by which the relatively large molecules in a feedstock such as VGO are converted to lighter fractions. This may be done by heating the VGO under non-oxidizing conditions, so-called thermal tracking. If done in the presence of a catalyst, the cracking process may be earned out at a lower temperature.
  • a major part of catalytic cracking is presently carried out in a fluid catalytic cracking process, or FCC process.
  • FCC process small particles of catalytic material are suspended in a lifting gas.
  • the feedstock is sprayed onto the catalyst particles through a nozzle.
  • the feedstock molecules are cracked on the catalyst particles.
  • the lift gas carries products and catalyst particles through the reactor.
  • the catalyst particles are separated from the reaction products, and sent to a stripping section where the catalyst is subjected to a severe steam treatment to remove as much of the hydrocarbon molecules as possible.
  • the catalyst particles are transferred to a regenerator where coke that was formed during the reaction is burned off, and the catalyst is regenerated for further use.
  • FCC processes have also been carried out in a downfiow reaction apparatus, e.g. a downer reactor.
  • a downfiow reaction apparatus e.g. a downer reactor.
  • back-mixing of hydrocarbons causes localized increases in residence time, which result in the enhancement of thermal cracking.
  • Thermal cracking increases undesirable dry gas make and decreases gasoline and light olefins production.
  • Down flow-type reaction zone may be employed to limit the amount of thermal cracking.
  • the catalyst in a standard FCC process comprises an acidic zeolite, such as Y- zeolite or a stabilized form of a Y-zeolite.
  • the Y-zeolite is combined with a matrix material, which may be alumina or silica-alumina.
  • the catalyst may further comprise components for improving its resistance against poisoning by metal contaminants of the feedstock, in particular nickel and vanadium. Other components may be present to capture sulfur from the feedstock.
  • the actual cracking process takes place on the acidic sites of the zeolite.
  • Dry gas is a low molecular weight fraction that does not liquefy when compressed at ambient temperature (hence the term dry).
  • the dry gas comprises hydrogen, methane, ethane and ethene.
  • the liquefied petroleum gas (LPG) fraction consists of compounds that are in the gas form at room temperature, but liquefy when compressed. This fraction comprises predominantly propane, propene, butane, and its mono- and di-olefms.
  • the gasoline fraction may have a boiling point range of from about the boiling point of nC 5 (36 0 C) to about 22O 0 C.
  • the endpoint may be varied to meet specific objectives of the refining process.
  • the gasoline fraction forms the basis of commercial gasoline sold as a fuel for vehicles equipped with an Otto engine.
  • One of the main requirements for the gasoline fraction is that it has as high an octane number as possible.
  • Straight-chain hydrocarbons have a low octane number; branched-chain hydrocarbons have a higher octane number, with the octane number further increasing with the number of alkyl groups.
  • Olefins have a high octane number, and aromatics have an even higher octane number.
  • the light cycle oil fraction forms the basis for fuel oil. It is the fraction having a boiling point above that of the gasoline fraction and lower than about 340 0 C. Hydrotreatment is required to convert the LCO to diesel fuel.
  • the quality of the LCO in terms of its nitrogen content, its sulfur content and its aromatics content, determine the rate at which the LCO fraction may be blended into the feed that will be converted to diesel fuel in the hydrotreatment process. It is important for diesel fuel to have as high a cetane number as possible. Straight-chain hydrocarbons have a high cetane number; branched-chain hydrocarbons, olefins and aromatics have low cetane numbers.
  • the product fraction having a boiling point above about 34O 0 C is referred to as "bottoms" or slurry.
  • bottoms or slurry.
  • the composition of the product mix is adversely affected by operating at high conversion rates.
  • the coke yield increases as the conversion increases.
  • Coke is a term describing the formation of carbon and pre-carbon deposits onto the catalyst. Up to a point, the formation of coke is essential to the cracking process as it provides the energy for the endothermic cracking reaction.
  • a high coke yield is, however, undesirable, because it results in a loss of hydrocarbon material and disruption of the heat balance as burning off of the coke produces more heat than the process requires. Under these conditions it may be necessary to release part of the produced heat, for example by providing a catalyst-cooling device in the regenerator, or to operate the process in a partial combustion mode.
  • HCO heavy cycle oil
  • the most desirable fractions of the FCC products stream are the light olefins, the gasoline fraction, and the LCO fraction.
  • the desired split between the last two is determined by the demand for diesel and gasoline, and by the seasonal demand for heating fuel.
  • US 2005/0121363 discloses an FCC process wherein hydrotalcite-like compounds are used as an additive for reducing sulfur in gasoline. Small amounts of hydrotalcite-like compounds are used in combination with a catalyst comprising a large pore acidic zeolite, such as E-cat.
  • US 3,904,550 discloses a catalyst support comprised of alumina and aluminum phosphate.
  • the support is used for catalysts useful in hydrodesulfurization and hydrodenitrogenation processes.
  • the support material may also be combined with acidic zeolitic materials for use in hydrocracking or catalytic cracking.
  • the present invention is believed to be based on the discovery that a catalyst having basic sites catalyzes the cracking reaction via a radical, or one-electron, mechanism. This is the same mechanism as occurs in thermal cracking. The difference with thermal cracking is that the presence of a catalyst increases the rate of reaction, making it possible to operate at lower reaction temperatures as compared to thermal cracking.
  • the traditional FCC processes use an acidic material, commonly an acidic zeolite, as the cracking catalyst. The acidic sites of the catalyst catalyze the cracking reaction via a two-electron mechanism.
  • the most preferred catalyst composition is one that is substantially free of large pore zeolite.
  • the catalyst in a standard FCC process comprises an acidic large pore zeolite, such as Y- zeolite or a stabilized form of a Y-zeolite.
  • the Y-zeolite is combined with a matrix material, which may be alumina or silica-alumina.
  • the presence of the large pore zeolite improves FCC gasoline octane by increasing aromaticity.
  • Intermediate pore and/or small pore zeolites have been added to conventional FCC catalysts to increase production of LPG, particularly propylene.
  • the effect of intermediate pore and/or small pore zeolite is limited due to the high aromatization tendency of the large pore zeolite.
  • the quality of the FCC gasoline fraction from the reactor becomes olefmic and very unstable.
  • These olefins may be converted into LPG by employing intermediate and/or small pore zeolite.
  • one benefit of a basic FCC catalyst blend reduced aromaticity, may be combined with one benefit of intermediate and/or small pore zeolite to produce an FCC gasoline fraction having acceptable olefmicity, an LCO fraction having acceptable aromaticity, and/or increased propylene production.
  • the bottoms fraction will also be less aromatic as compared to conventional FCC catalysts yields.
  • the bottoms fraction can be more easily recycled to the reactor or to a higher severity FCC operation.
  • the bottoms fraction may also be hydrotreated prior to catalytic cracking, or may be processed in a hydrocracker.
  • the present invention in one embodiment, is a catalytic composition comprising a basic material and an intermediate and/or small pore zeolite, wherein the catalytic composition is substantially free of large pore zeolite.
  • catalytic composition refers to the combination of catalytic materials that is contacted with an FCC feedstock in an FCC process.
  • the catalytic composition may consist of one type of catalytic particles, or may be a combination of different types of particles.
  • the catalytic composition may comprise particles of a main catalytic material and particles of a catalyst additive.
  • the combined composition should contain very little large pore zeolite, and is preferably substantially free of large pore zeolite.
  • the catalyst compositions described herein are employed in a down-flow type reaction zone, e.g., a downer reactor.
  • Materials suitable for use as catalytic compositions in the present invention include basic materials (both Lewis bases and Bronstedt bases), solid materials having vacancies, transition metals, and phosphates. It is desirable that the materials have a low dehydrogenating activity and do not catalyze hydrogen transfer.
  • the catalytic compositions of the present invention are substantially free of components having a dehydrogenating activity.
  • a dehydrogenating activity For example, it has been discovered, that compounds of several transition metals tend to have too strong a dehydrogenation activity to be useful in this context. Although they may possess the required basic character, the dehydrogenation activity of these materials results in an undesirably high coke yield and formation of too much aromatics.
  • transition metals that tend to be present in or convert to their metallic state under FCC conditions have too high a dehydrogenation activity to be useful for the present purpose.
  • the basic material may be supported on a suitable carrier.
  • the basic material may be deposited on the carrier by any suitable method known in the art.
  • the carrier material may be acidic in nature. In many cases the basic material will cover the acidic sites of the carrier, resulting in a catalyst having the required basic character.
  • Suitable carrier materials include the refractory oxides, in particular alumina, silica, silica- alumina, titania, zirconia, and mixtures thereof.
  • Suitable basic materials for use in the catalytic compositions of the present invention include compounds of alkali metals, compounds of alkaline earth metals, compounds of trivalent metals, compounds of transition metals, compounds of the Lanthanides, and mixtures thereof.
  • Suitable compounds include the oxides, the hydroxides and the phosphates of these elements.
  • a class of materials preferred as basic materials in the catalytic compositions of the present invention are mixed metal oxides, mixed metal hydroxides, and mixed metal phosphates.
  • Cationic and anionic layered materials are suitable as precursors to mixed metal oxides.
  • Another group of preferred basic materials for the present invention are compounds of transition metals, in particular the oxides, hydroxides and phosphates. Preferred are compounds of transition metals that do not have a strong dehydrogenation activity. Examples of suitable materials include ZrO 2 , Y 2 O 3 , and Nb 2 Os.
  • a preferred class of materials for use as basic catalytic compositions in the present invention are anionic clays, in particular hydrotalcite-like materials.
  • the brucite-like main layers are built up of octahedra alternating with interlayers in which water molecules and anions, more particularly carbonate ions, are distributed.
  • the interlayers may contain anions such as NO 3 “ , OH “ , Cl “ , Br “ , I “ , SO 4 “ , SiO 3 “ , CrO 4 2” , BO 3 2” , MnO 4 " , HGaO 3 2” , HVO 4 2” , ClO 4 " , BO 3 2” , pillaring anions such as Vi 0 O 2S 6" , monocarboxylates such as acetate, dicarboxylates such as oxalate, alkylsulfonates such as laurylsulfonate.
  • anions such as NO 3 " , OH “ , Cl “ , Br “ , I “ , SO 4 “ , SiO 3 “ , CrO 4 2” , BO 3 2” , MnO 4 " , HGaO 3 2” , HVO 4 2” , ClO 4 " , BO 3 2”
  • pillaring anions such as Vi 0 O 2S 6
  • True hydrotalcite that is hydrotalcites having magnesium as the divalent metal and alumina as the trivalent metal, is preferred for use in the present invention.
  • the catalytic selectivity of a hydrotalcite-like material may be improved by subjecting the hydrotalcite to heat deactivation.
  • a suitable method for heat deactivating a hydrotalcite material comprises treating the material in air or steam for several hours, for example five to 20 hours, at a temperature of from 300 to 900 0 C. Heating causes the layered structure to collapse and amorphous material to be formed. Upon continued heating, a doped periclase structure is formed, in which some of the Mg 2 ⁇ sites are filled with Al 3+ . In other words, vacancies are formed, which have been found to improve the selectivity of the catalytic material.
  • Another preferred class of basic materials is the aluminum phosphates.
  • the activity and the selectivity of the above-mentioned materials may be adjusted by doping these materials with another metal.
  • transition metals are suitable dopants for use in this context. Notable exceptions include those transition metals that have a dehyctrogenating activity, such as nickel, and the platinum group metals. Fe and Mo have also been found to be unsuitable.
  • Preferred dopants include metal cations from Groups lib, HIb, IVb of the Periodic Table of elements, and the rare earth metals.
  • Specifically preferred dopants include La, W, Zn, Zr, and mixtures thereof.
  • the catalytic compositions of the present invention may further comprise an acidic material, provided that the overall character of the catalyst remains predominantly basic.
  • the term "predominantly basic” is used herein to mean that less than about 40% of the material's sites are acidic. This is because the overall character of the material tends to become acidic under this condition. The presence of a material having acidic sites may be desirable in terms of improving the overall activity of the catalyst.
  • Silica-magnesia is an example of a material having both basic and acidic sites.
  • Suitable predominately basic materials having acidic sites include silica sol, metal doped silica sol, and nano-scale composites of silica with other refractory oxides.
  • Zeolites are crystalline aluminosilicates which have a uniform crystal structure characterized by a large number of regular small cavities that can be interconnected by a large number of even smaller rectangular channels. It was discovered that, by virtue of this structure consisting of a network of interconnected uniformly sized cavities and channels, crystalline zeolites are able to accept for absorption molecules having sizes below a certain well defined value whilst rejecting molecules of larger size, and for this reason they have come to be known as "molecular sieves.” This characteristic structure also gives them catalytic properties, especially for certain types of hydrocarbon conversions.
  • Intermediate and smaller pore zeolites are characterized by having an effective pore opening diameter of less than or equal to 0.7 nm, rings of 10 or fewer members and a Constraint Index of less than 31 and greater than 2.
  • Intermediate and/or small pore zeolites useful in the present invention include the ZSM family of zeolites, including but not limited to ZSM-5, ZSM-H, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48, and other similar materials.
  • Other suitable medium or smaller pore zeolites include ferrierite, erionite, and ST- 5, ITQ, and similar materials.
  • the crystalline aluminosilicate zeolite known as ZSM-5 is particularly described in U.S. Pat.
  • ZSM-5 crystalline aluminosilicate is characterized by a silica-to-alumina mole ratio of greater than 5 and more precisely in the anhydrous state by the general formula:
  • M having a valence n is selected from the group consisting of a mixture of alkali metal cations and organo ammonium cations, particularly a mixture of sodium and tetraalkyl ammonium cations, the alkyl groups of which preferably contain 2 to 5 carbon atoms.
  • anhydrous as used in the above context means that molecular water is not included in the formula.
  • the mole ratio Of SiO 2 to Al 2 O 3 for a ZSM-5 zeolite can vary widely.
  • ZSM-5 zeolites can be aluminum-free in which the ZSM-5 is formed from an alkali mixture of silica containing only impurities of aluminum.
  • AU zeolites characterized as ZSM-5 will have the characteristic X-ray diffraction pattern set forth in U.S. Pat. No. 3,702,886, regardless of the aluminum content of the zeolite.
  • any known process may be employed to produce the intermediate and/or small pore zeolites useful in the present invention.
  • Crystalline aluminosilicates in general have been prepared from mixtures of oxides including sodium oxide, alumina, silica and water. More recently clays and coprecipitated aluminosilicate gels, in the dehydrated form, have been used as sources of alumina and silica in reaction systems.
  • the catalytic compositions of the present invention should contain between about 1 to about 75 wt % of at least one intermediate and/or small pore zeolite with greater than about 5 wt % being preferred, greater than about 10% being more preferred.
  • the catalytic composition preferably comprises two distinct particles: one comprising a basic material and the other comprising the intermediate and/or small pore zeolite.
  • the catalytic compositions of the present invention preferably have a relatively high specific surface area, to compensate for their activity being lower than that of conventional FCC catalysts.
  • the catalytic compositions Preferably have a specific surface area as measured by the BET method after steam deactivation at 600 0 C for 2 hours of at least 60 m /g, preferably at least 90 m /g.
  • Another aspect of the present invention is an FCC process comprising the step of contacting an FCC feed stock with the catalytic composition of the present invention under FCC reaction conditions.
  • the FCC feed stock may be VGO, hydrotreated VGO, atmospheric resid, and mixtures thereof.
  • the term "FCC process" as used herein refers to process conditions that are typical for conventional FCC processes. Specifically, the temperature at the riser exit is less than about 600 0 C, preferably less than 55O 0 C; the total pressure is less than 2 bar, with the hydrogen partial pressure being even less than the total pressure. The conversion is typically less than 70%.
  • Figure 1 shows a typical FCC process arrangement employing a downer reactor.
  • the principal components of the FCC arrangement shown in Figure 1 consist of a reaction zone 1, a gas-solid separation zone 2, a stripping zone 3, a regeneration zone 4, a riser type regenerator 5, a catalyst hopper 6, and a mixing zone 7.
  • the arrangement circulates catalyst and contacts feed in the manner hereinafter described.
  • An FCC feedstock such as heavy gas oil
  • a mixture of regenerated catalyst and non-regenerated catalyst may be routed to mixing zone 7 to optimize reaction selectivity.
  • the mixture falls downward through the reaction zone 1, where the cracking reaction takes place under relatively high reaction temperatures and at relatively short contact times.
  • Water, steam, gasoline, gasoil, cycle oil, and/or slurry oil may be injected at any convenient point from the catalyst inlet to the outlet of reaction zone 1 for the purposes of quenching the reaction or for the purpose of recycling material from the FCC process or from an external source.
  • the mixture of spent catalyst and products from the reaction zone 1 enters the gas-solid separation zone 2 located under the reaction zone 1.
  • the spent catalyst is separated, in separation zone 2, from the cracked products and un-reacted feed.
  • the catalyst is then sent to the upper portion of the stripping zone 3 through dip leg 9.
  • Hydrocarbon gases separated from most of the spent catalyst are sent to a secondary separator 8, where the rest of the spent catalyst is separated from the product gas. Hydrocarbon gases are then sent to a product recovery section.
  • a tangential-type cyclone is preferred for use as the secondary separator 8.
  • Catalyst separated by the secondary separator 8 is directed to the stripping zone 3 where heavy hydrocarbons adsorbed on the catalyst are removed by a stripping gas introduced through line 11.
  • a stripping temperature of from about 500 to about 630 0 C and a catalyst residence time of from about 1 to about 10 minutes are preferred.
  • Vapors of cracked products and un- reacted feed oil, stripped from the spent catalyst in the stripping zone 3 are withdrawn through line 12 located at the top of the stripping zone, together with the stripping gas. These gases are then sent to a product recovery section.
  • the spent stripped catalyst is transferred to the regeneration zone through the line that has the first flow controller 13.
  • the superficial gas velocity in the stripping zone 3 is preferably maintained within the range of from about 0.05 to about 0.4 m/s, in order to keep the fluidized bed in the stripping zone in a bubble phase. Since the gas velocity is relatively low within the bubble phase zone, the consumption of stripping gas can be minimized. Moreover, the range of operational pressure of the first flow controller 13 may be broad, during the bubble phase condition, due to the high bed density, and therefore the transportation of catalyst particles from the stripping zone 3 to the regeneration zone 4 is facilitated. Perforated trays or other internal structures can be used in the stripping zone 3 to improve stripping efficiency between the stripping gas and the catalyst.
  • the spent catalyst is regenerated with a combustion gas (typically an oxygen- containing gas such as air), which is fed to the regeneration zone 4 through line 14. Regeneration is by burning, under fluidized conditions, the carbonaceous materials and heavy hydrocarbons, which have been adsorbed on the spent catalyst.
  • Catalyst regeneration temperature is normally in the range of from about 600 to about 1000 0 C.
  • Catalyst residence time in the regeneration zone 4 is in the range of from about 1 to about 5 minutes, and the superficial gas velocity is preferably in the range of from about 0.4 to about 1.2 m/s.
  • the regenerated catalyst from the riser-type regenerator 5 is carried to the catalyst hopper 6 located at the top of the riser type regenerator.
  • the catalyst hopper 6, which functions as a gas-solid separator, where the flue gases that contain the by-products of coke combustion are separated from the regenerated catalyst and removed through cyclone 15.
  • the regenerated catalyst in catalyst hopper 6 is routed to the mixing zone 7 through a downer line equipped with a second flow controller 17. If necessary, a portion of the regenerated catalyst in the catalyst hopper 6 can be returned back to the regeneration zone 4 through a bypass line equipped with a third flow controller 16.
  • reaction zone outlet temperature means an outlet temperature of the down flow-type reaction zone, and it is the temperature before separation of the cracked products from the catalysts, or, in the case that they are quenched just upstream of the separator, it is the temperature before quenching thereof.
  • the reaction zone outlet temperature is typically less than about 650 0 C.
  • the catalyst/oil ratio may range from about 15 to about 40 wt/wt, or greater.
  • the contact time referred to herein means either the time between the start of contact of the feed oil with the regenerated catalysts and the separation of the produced cracked products from the catalysts, or, the time between the start of contact of the feed oil with the regenerated catalysts and the quenching, in the case that the produced cracked products are quenched just upstream of the separation zone.
  • the contact time may be in the range of from about 0.1 to about 1 second.
  • FCC process does not encompass hydrotreatment processes, which require elevated hydrogen pressures on the order of 100 bar or more.
  • FCC process also does not encompass steam pyrolysis, which is carried out at temperatures above 600 0 C, and results in a conversion of more than 90%, typically (close to) 100%.
  • Hydrotalcite was prepared following the procedure described in US Patent 6,589,902. The Mg to Al ratio was 4:1. The hydrotalcite was calcined at 600 0 C for one hour. [0065] The catalytic activity and selectivity of the hydrotalcite and a blend of 60 wt% hydrotalcite and 40 wt% ZSM-5 was evaluated in a micro-activity reactor. VGO was used as feedstock. AU test reactions were performed at a contact temperature of 550 0 C.
  • the reaction product was subjected to distillation.
  • the light cycle oil fraction (LCO fraction) was separated and analyzed for total aromatics content using calibrated gas chromatography.
  • the coke yield was determined by analyzing the CO and CO 2 contents of the effluent of the regenerator under oxidizing conditions.

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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)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)

Abstract

L'invention porte sur de nouvelles compositions catalytiques pour le craquage de fractions de pétrole brut. Les compositions catalytiques comprennent une matière basique et au moins une zéolite à pores de dimension intermédiaire et/ou de petite dimension et comprennent peu à pas de zéolite à pores de grande dimension.
PCT/IB2009/005002 2008-01-09 2009-01-07 Procédé de craquage catalytique fluide employant des compositions de craquage basiques Ceased WO2009087576A2 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4396538A (en) * 1979-09-04 1983-08-02 Mobil Oil Corporation Hydrotreating/hydrocracking catalyst
GB8718108D0 (en) * 1987-07-30 1987-09-03 Unilever Plc Petroleum catalysts
US5944982A (en) * 1998-10-05 1999-08-31 Uop Llc Method for high severity cracking
US20020195373A1 (en) * 2001-06-07 2002-12-26 Takashi Ino Heavy oil fluid catalytic cracking process
BR0210168A (pt) * 2001-06-08 2004-04-27 Petroleo Brasileiro Sa Processo para craqueamento catalìtico fluido
US7431825B2 (en) * 2003-12-05 2008-10-07 Intercat, Inc. Gasoline sulfur reduction using hydrotalcite like compounds
TWI277648B (en) * 2004-07-29 2007-04-01 China Petrochemical Technology A cracking catalyst for hydrocarbons and its preparation
KR20080081048A (ko) * 2005-12-22 2008-09-05 알베마를 네덜란드 비.브이. 신규 분해 촉매 조성물
WO2008148686A1 (fr) * 2007-06-08 2008-12-11 Albemarle Netherlands, B.V. Craquage catalytique et procédé d'hydrotraitement pour un rendement de diesel élevé avec une faible teneur en aromatiques et/ou un rendement de propylène élevé

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WO2009087576A9 (fr) 2010-02-04

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