WO2009087576A2

WO2009087576A2 - Fcc process employing basic cracking compositions

Info

Publication number: WO2009087576A2
Application number: PCT/IB2009/005002
Authority: WO
Inventors: Elbert Arjan De Graaf; Leendert Arie Gerritsen
Original assignee: Albemarle Netherlands B.V.
Priority date: 2008-01-09
Filing date: 2009-01-07
Publication date: 2009-07-16
Also published as: WO2009087576A3; WO2009087576A9

Abstract

Novel catalytic compositions for cracking of crude oil fractions are disclosed. The catalytic compositions comprise a basic material and at least one intermediate and/or small pore zeolite, and comprises little to no large pore zeolite.

Description

FCC PROCESS EMPLOYING BASIC CRACKING COMPOSITIONS

[0001] Crude oil is a complex mixture of hydrocarbons. In a refinery, 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. Other feedstocks for cracking process include among others hydrotreated VGO and atmospheric resid.

[0002] 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.

[0003] A major part of catalytic cracking is presently carried out in a fluid catalytic cracking process, or FCC process. In this 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. After the reaction 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. After the stripper, 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.

[0004] FCC processes have also been carried out in a downfiow reaction apparatus, e.g. a downer reactor. In riser reactors, 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.

[0005] The catalyst in a standard FCC process comprises an acidic zeolite, such as Y- zeolite or a stabilized form of a Y-zeolite. Generally, 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.

[0006] The product of the FCC process is subsequently split into several fractions. 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.

[0007] The gasoline fraction may have a boiling point range of from about the boiling point of nC₅ (36⁰C) to about 22O⁰C. 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.

[0008] The light cycle oil fraction, or LCO 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 340⁰C. Hydrotreatment is required to convert the LCO to diesel fuel.

[0009] 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.

[0010] The product fraction having a boiling point above about 34O⁰C is referred to as "bottoms" or slurry. Although it is desirable to operate at the highest possible conversion, the composition of the product mix is adversely affected by operating at high conversion rates. For example, 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.

[0011] The fraction of the bottoms having a boiling point between about 340 and about 496°C is referred to as heavy cycle oil, or HCO.

[0012] In general, 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.

[0013] Because of the need for a high cetane number, it is desirable to keep the amount of aromatics in the light cycle oil fraction as low as possible. In terms of their boiling points, a large portion of any aromatics formed in FCC will end up in the light cycle oil fraction. It is therefore desirable to minimize the amount of aromatics that is formed in the cracking process.

[0014] Lighter aromatics, such as benzene and toluene, become part of the gasoline fraction of the product stream. Because of their high octane numbers, the aromatic components of gasoline might be considered desirable. However, because of a growing concern about the toxicity of aromatic compounds, it has become desirable to form a gasoline fraction that is low in aromatics content. The octane number of the gasoline pool of the refinery can be increased by alkylation of the butylenes and the isobutane streams from the FCC. Additional isobutane may be needed from other refinery processes. The high quality alkylate has also a desirable very low aromatics content, thereby reducing the aromatics content of the total gasoline pool.

[0015] US 2005/0121363 (Vierheilig et al.) 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.

[0016] US 3,904,550 (Pine) 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.

[0017] It is desirable to develop a catalyst for use in a cracking process for the cracking of FCC feed stock whereby the formation of aromatics in the light cycle oil fraction is reduced, as compared to conventional FCC processes, without deleterious effects to the olefmic characteristics of the FCC gasoline fraction.

[0018] While not being bound by any proposed theory, 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. By contrast, 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. This mechanism favors the formation of high molecular weight olefins, which readily become cyclized to form cycloalkanes. The cycloalkanes in turn readily react to aromatics via hydrogen transfer catalyzed by the large pore zeolites. The amount and properties of large pore zeolites, such as USY, REY and others known in the art, determine the extent of this reaction. Even small amounts of large pore zeolites increase the activity of the catalyst system significantly, however at the cost of LCO quality. Therefore, the amount of large pore zeolite in the catalyst blend is preferably less than 15%, more preferably less than 10% and more preferably is less than 5% zeolite. The most preferred catalyst composition is one that is substantially free of large pore zeolite.

[0019] As stated above, 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. Generally, 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. However, the effect of intermediate pore and/or small pore zeolite is limited due to the high aromatization tendency of the large pore zeolite.

[0020] When the nature of the FCC catalyst blend is basic, 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. Thus, 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. These effects may be particularly pronounced when employed in a down-flow type reaction zone.

[0021] In addition, the bottoms fraction will also be less aromatic as compared to conventional FCC catalysts yields. Thus, 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.

[0022] Accordingly, 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. The term "catalytic composition" as used herein 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. For example, 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.

[0023] In one preferred embodiment, the catalyst compositions described herein are employed in a down-flow type reaction zone, e.g., a downer reactor.

[0024] The catalytic compositions of the present invention provide a conversion of FCC feed stock of at least 10% at a catalyst-to-oil (CTO) ratio of 10 and a riser outlet temperature below 700⁰C. Conversion is defined as (dry gas) + (LPG) + (Gasoline) + (Coke) = 100 - (Bottoms) - (LCO). Preferably the conversion is at least 20%, more preferably at least 30%. [0025] 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. Preferably, the catalytic compositions of the present invention are substantially free of components having 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. As a general rule, 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.

[0026] The basic material may be supported on a suitable carrier. For this purpose the basic material may be deposited on the carrier by any suitable method known in the art.

[0027] 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.

[0028] 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.

[0029] Suitable compounds include the oxides, the hydroxides and the phosphates of these elements.

[0030] 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.

[0031] 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 ZrO₂, Y₂O₃, and Nb₂Os.

[0032] A preferred class of materials for use as basic catalytic compositions in the present invention are anionic clays, in particular hydrotalcite-like materials.

[0033] In hydrotalcite-like anionic clays, 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.

[0034] The interlayers may contain anions such as NO₃ ^", OH^", Cl^", Br^", I^", SO₄ ^", SiO₃ ^", CrO₄ ^2", BO₃ ^2", MnO₄ ^", HGaO₃ ^2", HVO₄ ^2", ClO₄ ^", BO₃ ^2", pillaring anions such as Vi₀O_2S ^6", monocarboxylates such as acetate, dicarboxylates such as oxalate, alkylsulfonates such as laurylsulfonate.

[0035] "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.

[0036] The catalytic selectivity of a hydrotalcite-like material (including hydrotalcite itself) 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 900⁰C. 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 Al³⁺. In other words, vacancies are formed, which have been found to improve the selectivity of the catalytic material.

[0037] Extreme heat treatment will cause this material to segregate into a periclase and a spinel structure. The spinel structure is inactive as a catalyst. Significant spinel formation has been observed after heating a hydrotalcite material for four hours at 900⁰C.

[0038] Another preferred class of basic materials is the aluminum phosphates.

[0039] The activity and the selectivity of the above-mentioned materials may be adjusted by doping these materials with another metal. In general, most 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.

[0040] 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.

[0041] 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.

[0042] Silica-magnesia is an example of a material having both basic and acidic sites.

[0043] Suitable predominately basic materials having acidic sites include silica sol, metal doped silica sol, and nano-scale composites of silica with other refractory oxides.

[0044] 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.

[0045] 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. No. 3,702,886; the disclosure of which is incorporated herein by reference. 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:

[0.9±0.2M_2/tlO: Al₂O₃ :>5SiO₂]

[0046] wherein 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. The term "anhydrous" as used in the above context means that molecular water is not included in the formula. In general, the mole ratio Of SiO₂ to Al₂O₃ for a ZSM-5 zeolite can vary widely. For example, 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, however, 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.

[0047] 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.

[0048] A suitable method for preparing a catalyst having a high attrition resistance is described in US Patent 6,589,902 to Stamires et al., the disclosures of which are incorporated herein by reference.

[0049] 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.

[0050] 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. Preferably the catalytic compositions have a specific surface area as measured by the BET method after steam deactivation at 600⁰C for 2 hours of at least 60 m /g, preferably at least 90 m /g. [0051] 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 600⁰C, preferably less than 55O⁰C; 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%.

[0052] 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.

[0053] An FCC feedstock, such as heavy gas oil, is charged to the mixing zone 7 through line 10, and is mixed with the regenerated catalyst from the catalyst hopper 6. Alternatively, 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.

[0054] 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.

[0055] 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. Steam produced in a boiler, or an inert gas such as nitrogen, pressurized in a compressor, is preferably used as the stripping gas. As stripping conditions, a stripping temperature of from about 500 to about 630⁰C 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.

[0056] 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.

[0057] 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 1000⁰C. 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.

[0058] After regeneration of the spent catalyst in the regeneration zone 4, the regenerated catalyst in the upper portion of the turbulent-phase fluidized bed is transferred to a riser-type regenerator s.

[0059] 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.

[0060] As described above, FCC catalyst circulates in the apparatus through 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 "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 650⁰C.

[0061] In down-flow type reactors, the catalyst/oil ratio may range from about 15 to about 40 wt/wt, or greater.

[0062] 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.

[0063] It will be understood that the term FCC process does not encompass hydrotreatment processes, which require elevated hydrogen pressures on the order of 100 bar or more. The term FCC process also does not encompass steam pyrolysis, which is carried out at temperatures above 600⁰C, and results in a conversion of more than 90%, typically (close to) 100%.

EXAMPLE

[0064] 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 600⁰C 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 550⁰C.

[0066] Characteristics of VGO

a) Simdist °C

5wt% 345

10wt% 365

20wt% 391

30wt% 409

40wt% 425

50wt% 445

60wt% 462

70wt% 488

80wt% 515

90wt% 548

95wt% 570

b) Saturates, wt% 63.7 c) Mono-Aromatics, wt% 16.3 d) Di-Aromatics, wt% 10,5 e) Di+Aromatics/Polars, wt% 9.5 f) Sulfur, ppmwt 6400 g) Nitrogen, ppmwt 1170 h) CCR, wt% 0.4

[0067] 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 CO₂ contents of the effluent of the regenerator under oxidizing conditions.

[0068] The table below illustrates that the addition of ZSM-5 decreases coke, gasoline and LCO yields, at the expense of bottoms yield. The increase in LPG yield is significant (136%), as is the change in dry gas composition. Yields are expressed as wt% of feed. In addition, the presence of the ZSM-5 only has a minor influence on the aromaticity of the LCO, contrary to blending large pore zeolites, such as in conventional FCC catalyst compositions. LCO composition is expressed as wt% of LCO fraction.

Claims

CLAIMS:

1. A process for the fluid catalytic cracking of a hydrocarbon feed, the process comprising contacting the oil with a FCC catalytic composition comprising a predominantly basic material and at least one intermediate or small pore zeolite, wherein the catalytic composition comprises less than 15 wt% large pore zeolite, wherein the contacting takes place in a fluid catalytic cracking apparatus having a regeneration zone, a down flow reaction zone, a separation zone and a stripping zone.

2. The process of claim 1, wherein the cracking occurs under conditions such that the reaction zone outlet temperature is less than about 650°C, the catalyst/oil ratio ranges from about 15 to about 40 wt/wt, and the contact time of hydrocarbons in the reaction zone ranges from about 0.1 to about 1 second.

3. The process of any of the preceding claims, wherein the catalytic composition comprises less than 10 wt% large pore zeolite.

4. The process of any of the preceding claims, wherein the catalytic composition comprises less than 5 wt% large pore zeolite.

5. The process of any of the preceding claims, wherein the catalytic composition is substantially free of large pore zeolite.

6. The process of any of the preceding claims, wherein the basic material is substantially free of components having a dehydrogenating activity or hydrogen transfer activity.

7. The process of any of the preceding claims, wherein the basic material is selected from the group consisting of compounds of alkali metals, compounds of alkaline earth metals, compounds of trivalent metals, compounds of transition metals, and mixtures thereof.

8. The process of any of the preceding claims, wherein the basic material is supported on a carrier material.

9. The process of any of the preceding claims, wherein the basic material is the oxide, the hydroxide or the phosphate of a transition metal, an alkali metal, an earth alkaline metal, or a transition metal, or a mixture thereof.

10. The process of any of claims 1 - 9, wherein the basic material comprises an alkali metal compound.

11. The process of any of claims 1 - 9, wherein the basic material comprises an alkaline earth metal compound.

12. The process of any of claims 1 - 9, wherein the basic material comprises a compound of a transition metal.

13. The process of claim 12 wherein the transition metal compound is selected from the group consisting of ZrO₂, Y₂O₃, Nb₂O₅, and mixtures thereof.

14. The process of any of claims 1 - 9, wherein the basic material is a mixed metal oxide.

15. The process of claim 14 wherein the basic material is a hydrotalcite.

16. The process of any of claims 1 - 9, wherein the basic material is an aluminum phosphate.

17. The process of any of claims 1 - 9, wherein the basic material is doped with a metal cation.

18. The process of claim 17 wherein the dopant metal cation is selected from metals of Group lib, Group HIb, Group IVb, the rare earth metals, and mixtures thereof.

19. The process of claim 18 wherein the dopant metal is selected from the group consisting of La, Zn, Zr, and mixtures thereof.

20. The process of claim 8 wherein the carrier is a refractory oxide.

21. The process of claim 20 wherein the carrier is selected from alumina, silica, silica-alumina, titania, and mixtures thereof.

22. The process of any of claims 1 - 9, further comprising a material having acidic sites.

23. The process of claim 22 wherein the material having acidic sites is selected from the group consisting of silica sol, metal doped silica sol, and nano-scale composites of silica with other refractory oxides.

24. The process of any of claims 1 - 9, wherein the at least one intermediate or small pore zeolite is selected from the ZSM family of zeolites.

25. The process of claim 24 wherein the ZSM family zeolite is ZSM-5.