Abstract: Methods and systems for producing pyrolysis products from a mixed plastics stream are described herein. The method may include conducting pyrolysis of a plastic feedstock to produce a stream of plastic pyrolysis oil; feeding a catalytic cracking feed stream and a catalyst from a catalyst regenerator into a fluidized bed reactor, where the catalytic cracking feed stream comprises the plastic pyrolysis oil; cracking the catalytic cracking feed stream in the fluidized bed reactor to produce a product stream and a spent catalyst; and transporting the spent catalyst to the catalyst regenerator and regenerating the catalyst in the catalyst regenerator. The product stream comprises olefins having a carbon number of C2-C4 and distillate fuel.

Abstract: Provided is a Fluid Catalytic Cracking catalyst additive composition and method of making the same. The catalyst additive composition comprises zeolite about 35 wt % to about 80 wt %, preferably about 40 wt % to about 70 wt %; silica about 0 wt % to about 10 wt %, preferably about 2 wt % to about 10 wt %; about 10.5 wt % to 20 wt % alumina and about 7 wt % to 20 wt % P2O5, preferably about 11 wt % to about 18 wt %, and the balance clay which can fall between 0 and 50 wt %. The alumina is typically derived from more than one source, such as at least an amorphous or small crystallite size pseudo-boehmite alumina and then either a large crystallite size alumina or other reactive alumina.

Abstract: The present disclosure concerns a process for converting methyl halides to ethylene and propylene, said process comprising the steps of (a) providing a feedstream comprising methyl halides; (b) providing a first and second catalyst composition, said second catalyst composition comprising a cracking catalyst; (c) contacting said feedstream with said first catalyst composition in a first reaction zone under first reaction conditions to provide a first product stream; and (d) subjecting at least a part of said first product stream to an Olefin Catalytic Cracking with said second catalyst composition in a second reaction zone under second reaction conditions to provide a second product steam. The process is remarkable in that said step (c) is performed under 400° C., and in that said first catalyst composition comprises molecular sieves with a Si/Al atomic between 2 and 18 and with a plurality of pores with a shape of an 8-membered ring or less.

Abstract: A process for upgrading a hydrocarbon feed to produce light olefins, includes contacting the hydrocarbon feed with steam in the presence of a cracking catalyst in a steam catalytic cracking reactor at reaction conditions sufficient to cause at least a portion of the hydrocarbons in the hydrocarbon feed to undergo one or more cracking reactions to produce a steam catalytic cracking effluent comprising ethylene, propylene, or both, wherein the process is capable of being transitioned between an ethylene-selective mode and a propylene-selective mode; determining whether to produce ethylene or propylene; when producing ethylene, then operating the process in ethylene-selective mode comprises producing more ethylene than propylene; or when producing propylene, then operating the process in propylene-selective mode comprises producing more propylene than ethylene.

Abstract: The present disclosure concerns an electron microscopy method, including the emission of a precessing electron beam and the acquisition, at least partly simultaneous, of an electron diffraction pattern and of intensity values of X rays.

Abstract: In a thermochemical regenerator wherein gaseous combustion products that are formed by combustion in a furnace are passed from the furnace into and through a first regenerator, the combustion products are combined with gaseous fuel, and the resulting mixture is passed into and through a second regenerator wherein the mixture undergoes an endothermic reaction to form syngas, the thermochemical regeneration is enhanced by injecting fuel gas into a recycle stream comprising the combustion products from the first regenerator to entrain recycled flue gas that passes out of the first regenerator and to impel the mixture into the other regenerator.

Abstract: A process for producing olefins from the hydrocarbon feed includes introducing the hydrocarbon feed into a Solvent Deasphalting Unit (SDA) to remove asphaltene from the hydrocarbon feed producing a deasphalted oil stream, wherein the SDA comprises a solvent that reacts with the hydrocarbon feed, and the deasphalted oil stream comprises from 0.01 weight percent (wt. %) to 18 wt. % asphaltenes; introducing the deasphalted oil stream into a steam catalytic cracking system; steam catalytically cracking the deasphalted oil stream in the steam catalytic cracking system in the presence of steam and a nano zeolite cracking catalyst to produce a steam catalytic cracking effluent; and separating the olefins from the steam catalytic cracking effluent.

Abstract: A hydrodesulfurization catalyst, which includes (i) a catalyst support including a zeolite doped with 0.1 to 0.5 wt. % of a graphene material, based on a total weight of the catalyst support, (ii) 5 to 20 wt. % of molybdenum, based on a total weight of the hydrodesulfurization catalyst, and (iii) 1 to 6 wt. % of a promoter selected from the group consisting of cobalt and nickel, based on a total weight of the hydrodesulfurization catalyst. The molybdenum and the promoter are homogeneously disposed on the catalyst support. A method of producing the hydrodesulfurization catalyst via incipient wetness impregnation techniques, and a method for desulfurizing a hydrocarbon feedstock with the hydrodesulfurization catalyst are also provided.

Abstract: A method for producing a fluoride functionalized zeolite catalyst is described, having a F/Si molar ratio of 0.1:1-3:1. The method involves mixing a fluoride salt with zeolite components to form a gel, which is then hydrothermally treated and calcined. The fluoride functionalized zeolite catalyst may be used for cracking an olefin stream into ethylene, propylene, and butylene, with high selectivity towards propylene. The fluoride functionalized zeolite catalyst may be used for 50 or more hours with a stable conversion rate and low coke formation.

Abstract: Hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof are dehydrated using a catalyst and a method to produce bio-acrylic acid, acrylic acid derivatives, or mixtures thereof. A method to produce the dehydration catalyst is also provided.

Abstract: A lower olefin by using a zeolite catalyst, a composite catalyst capable of further extending the lifetime of catalytic activity, a method for producing the composite catalyst, a method for producing a lower olefin by using the composite catalyst, and a method for regenerating a composite catalyst in the method for producing a lower olefin are provided. The composite catalyst is a catalyst for producing a lower olefin from a hydrocarbon feedstock. This composite catalyst is constituted of a zeolite being a crystalline aluminosilicate containing gallium and iron or iron and further having a framework with 8- to 12-membered ring, and of silicon dioxide. By using the composite catalyst, a lower olefin can be continuously produced over a long period of time.

Abstract: A joined body 10 includes a ceramic body 12, a metal member 14, and a joint portion 15 that joins the ceramic body 12 and the metal member 14 together. The joint portion 15 includes a first joint layer 16 joined to the ceramic body 12 and a second joint layer 18 joined to the metal member 14. The first joint layer 16 is disposed on the ceramic body 12 side and contains an alloy that contains Fe and Cr as main components, and a compound having a thermal expansion coefficient of 4.0×10?6 (/° C.) or lower is dispersed in the first joint layer 16. The second joint layer 18 is disposed on the metal member 14 side, contains an alloy that contains Fe and Cr as main components, and has a larger thermal expansion coefficient than the first joint layer 16.

Abstract: Systems and methods are provided for slurry hydroconversion of a heavy oil feed, such as an atmospheric or vacuum resid. The systems and methods allow for slurry hydroconversion using catalysts with enhanced activity. The catalysts with enhanced activity can be used in conjunction with demetallization catalysts or catalysts that can be recycled as a side product from a complementary refinery process.

Abstract: The present invention relates to a process for the dehydration of at least an alcohol to make at least an olefin, comprising: introducing in a reactor a stream (A) comprising at least an alcohol, optionally water, optionally an inert component, contacting said stream with a catalyst in said reactor at conditions effective to dehydrate at least a portion of the alcohol to make an olefin, recovering from said reactor an olefin containing stream (B), Wherein the catalyst is: a crystalline silicate having a ratio Si/Al of at least about 100, or a dealuminated crystalline silicate, or a phosphorus modified zeolite, the WHSV of the alcohols is at least 2 h?1, the temperature ranges from 280° C. to 500° C. It relates also to the same process as above but wherein the catalyst is a phosphorus modified zeolite and at any WHSV. The partial pressure of the alcohol in the dehydration reactor advantageously ranges from 1.2 to 4 bars absolute (0.12 MPa to 0.

Abstract: One exemplary embodiment can be a fluid catalytic cracking system. The system can include a reaction zone, in turn including a reactor receiving, a fluidizing stream, a fuel gas stream, a fluidizable catalyst, a stream having an effective amount of oxygen for combusting the fuel gas stream, and a feed.

Abstract: The invention relates to a rotary disc device (1) in a rotary fluidised bed, the outer edge of said disc rotating inside, and faster than, the fluidised bed, thereby allowing: the rotation speed of the fluidised bed to be accelerated, solid particles and/or micro-droplets to be supplied to the fluidised bed or to the free central area, and different annular areas of the fluidised bed to be separated. The invention also relates to methods for transforming solid particles or micro-droplets on contact with the fluids flowing through the rotary fluidised bed or for transforming fluids on contact with solids in suspension in the rotary fluidised bed, using said device.

Abstract: A process for the preparation of a naphtha-selective hydrocracking catalyst comprising of from 3 to 4.8% wt of molybdenum, calculated as metal, and of from 1.5 to 3% wt of nickel, calculated as metal, which comprises loading a refractory oxide support comprising an alumina binder component and a zeolite Y component in a content of from 65 to 75 wt % based on the total weight of the catalyst, with nickel and molybdenum in the presence of citric acid, wherein the zeolite Y component has a unit cell size in the range of from 24.42 to 24.52 ?, a SAR in the range of from 8 to 15, and a surface area of from 850 to 1020 m2/g.

Abstract: Additives for mixing into the base catalyst inventory of the fluid catalytic cracking (FCC) process units, so as to achieve a high selectivity of light olefins (ethylene and propylene), are described. Such additives comprise an FER zeolite and an MFI zeolite, the MFI zeolite preferably being zeolite ZSM-5. The mixture of the additive in a concentration greater than 2% w/w relative to the base catalyst of an FCC unit allows greater selectivity for light olefins, propylene and ethylene, while maintaining catalytic activity.

Abstract: One exemplary embodiment can be a process for fluid catalytic cracking. The process may include providing a first feed having a boiling point of about 180-about 800° C. to a first riser reactor, and providing a second feed having first and second parts to a second reactor. Typically, the first part includes one or more C5-C12 hydrocarbons and a second part includes one or more C4-C5 hydrocarbons. Generally, an effective amount of the second part is combined with the first part to maximize production of propene.

Abstract: One exemplary embodiment can be a fluid catalytic cracking system. Generally, the fluid catalytic cracking system includes a first reaction vessel and a second reaction vessel. The first reaction vessel may contain a first catalyst having pores with openings greater than about 0.7 nm and a second catalyst having pores with smaller openings than the first catalyst. What is more, the second reaction vessel may contain the second catalyst. Generally, at least a portion of the second catalyst is directly communicated with the first reaction vessel.

Abstract: The invention provides a catalyst for thermal decomposition of an organic substance having the form of spherical granule having a particle diameter of 0.1 to 1.2 mm, a pore volume of 0.1 to 0.3 mL/g, a tap density of 1.05 to 1.4 g/mL, and a wear rate of 2% by weight or less, the catalyst being obtained by mixing and granulating a pulverized product of an inorganic oxide exemplified by titanium oxide with at least one sol selected from a titania sol, a silica sol, an alumina sol, and a zirconia sol to make spherical granules, calcining the spherical granules at a temperature from 400 to 850° C., and sieving the calcined granules.

Abstract: The invention concerns a process for the production of gasoline and for the co-production of propylene using a catalytic cracking unit comprising a catalyst regeneration zone and a reaction zone with two risers functioning in parallel under different severity conditions, the catalyst circulating between the regeneration zone and the reaction zone in two parallel circuits, a circuit termed the principal circuit comprising a first external catalyst cooling system, and a circuit termed the secondary circuit comprising a second external catalyst cooling system.

Abstract: One exemplary embodiment can be a fluid catalytic cracking system. The system can include a reaction zone, in turn including a reactor receiving, a fluidizing stream, a fuel gas stream, a fluidizable catalyst, a stream having an effective amount of oxygen for combusting the fuel gas stream, and a feed.

Abstract: A process is described for maximization of light olefins, preferably ethylene, by the catalytic cracking of feeds of saturated hydrocarbons, with molecular size in the range from 4 to 6 carbon atoms. The process uses a catalyst based on a zeolite of type ZSM-5 with low sodium content and modified with nickel, with concentration by weight of nickel, expressed in the form of oxide, in the range from 0.1% to 20% relative to the weight of zeolite in the catalyst, and operating conditions that involve a temperature between 400° C. and 650° C. and feed partial pressure between 0.1 and 1.0 MPa, so that the product recovered is rich in light olefins, with ethylene/propylene ratio in the range from 0.25 to 2.00.

Abstract: 1-butene is recovered as a purified product from an MTO synthesis and especially from an integrated MTO synthesis and hydrocarbon pyrolysis system in which the MTO system and its complementary olefin cracking reactor are combined with a hydrocarbon pyrolysis reactor in a way that facilitates the flexible production and recovery of olefins and other petrochemical products, particularly butene-1 and MTBE.

Abstract: One exemplary embodiment can be a fluid catalytic cracking system. The system can include a reaction zone, in turn including a reactor receiving, a fluidizing stream, a fuel gas stream, a fluidizable catalyst, a stream having an effective amount of oxygen for combusting the fuel gas stream, and a feed.

Abstract: The present invention relates to a process for the oxidative regeneration of a deactivated catalyst comprising molecular sieve to provide a regenerated molecular sieve catalyst, wherein said deactivated catalyst is from one or both of an oxygenate to olefin process and a olefin cracking process, said regeneration process comprising at least the steps of providing a regeneration gas stream comprising oxidant; treating the regeneration gas stream with a liquid adsorbent stream comprising an ethylene glycol in a contaminant absorption zone to remove at least a part of one or more of any water, any alkali metal ion and any alkaline earth metal ion present in the regeneration gas stream to provide a treated regeneration gas stream comprising oxidant; regenerating a deactivated catalyst comprising molecular sieve with the treated regeneration gas stream to provide a regenerated catalyst comprising regenerated molecular sieve.

Abstract: The present invention relates to a process for the oxidative regeneration of a deactivated catalyst comprising providing a catalyst comprising molecular sieve in hydrogen form to a guard zone; passing a regeneration gas stream comprising oxidant through the guard zone to remove part of one or both of any alkali metal ion and alkaline earth metal ion from the regeneration gas stream, to provide a treated regeneration gas stream; providing deactivated catalyst comprising molecular sieve in a regeneration zone, said deactivated catalyst from one or both of an oxygenate to olefin process and an olefin cracking process; regenerating the deactivated catalyst in the regeneration zone with the treated regeneration gas stream to provide regenerated molecular sieve catalyst; wherein said catalyst in said guard zone is one or both of deactivated catalyst comprising molecular sieve in hydrogen form and regenerated catalyst comprising regenerated molecular sieve in hydrogen form.

Abstract: Systems and methods for producing a hydrocarbon are provided. The method can include separating a hydrocarbon comprising olefins and paraffins to produce an olefin-rich hydrocarbon comprising about 70 wt % or more olefins and a paraffin-rich hydrocarbon comprising about 70 wt % or more paraffins. The method can also include cracking at least a portion of the olefin-rich hydrocarbon in the presence of one or more catalysts at conditions sufficient to produce a cracked product comprising about 20 wt % or more C2-C3 olefins.

Abstract: A catalyst can include a phosphorus modified zeolite having partly an ALPO structure. The ALPO structure can be determined by a signal between 35-45 ppm in 27Al MAS NMR spectrum. The zeolite can include at least one ten member ring in the structure thereof. The catalyst can also include a binder and one or more metal oxides. The catalyst can be used in processes in the presence of steam at high temperatures, such as temperatures that are above 300° C. and up to 800° C. The catalyst can be used in alcohol dehydration, olefin cracking, MTO processes, and alkylation of aromatic compounds with olefins and/or alcohols.

Abstract: The disclosure relates to catalytically active carbocatalysts, e.g., a graphene oxide or graphite oxide catalyst suitable for use in a variety of high value chemical transformations.

Abstract: A process for increasing the yield of C3 olefin in fluidized bed catalytic cracking of hydrocarbon feedstocks is disclosed. C4 fraction produced from the cracking of hydrocarbon feedstock in the primary reaction zone (riser), optionally with external source of C4 stream is fed into the stripper which acts as a secondary reaction zone at an elevated temperature and at an optimum WHSV. The elevated temperature is achieved by injecting a part of the regenerated catalyst from regenerator, which is at a higher temperature, directly into the stripper through a dedicated additional lift line. This raises the activity of catalyst inside the stripper. The direct injection of regenerated catalyst into the stripper, besides producing higher yields of propylene, improves the stripping efficiency leading to enhanced recovery of strippable hydrocarbons.

Abstract: A rotary machine type shock wave reactor suitable for thermal cracking of hydrocarbon-containing materials includes a casing, a rotor whose periphery contains an axial-flow blade cascade, and a directing rim, provided with at least two stationary vane cascades, adjoining an axial-flow rotor cascade, wherein the casing substantially encloses the periphery of the rotor and the directing rim. The cascades are configured to direct feedstock containing process stream to repeatedly pass the cascades in a helical trajectory while propagating within the duct between the inlet and exit and to generate stationary shock-waves to heat the feedstock. The axial-flow rotor cascade is configured to provide kinetic energy and add velocity to feedstock containing process stream, and the stationary vanes located downstream the rotor cascade are configured to reduce the velocity of the stream and convert kinetic energy into heat.

Abstract: A method to make a phosphorus modified zeolite can include providing a zeolite including at least one ten member ring in the structure steaming the zeolite, mixing the zeolite with one or more binders and shaping additives, and then shaping the mixture. The method can include making a ion-exchange. The shaped mixture can be steamed. Phosphorous can be introduced on the catalyst to introduce at least 0.1 wt % of phosphorus, such as be dry impregnation or chemical vapor deposition. A metal, such as calcium, can be introduced. The catalyst can be washed, calcinated, and then steamed. The steaming severity (X) can be at least about 2. The catalyst can be steamed at a temperature above 625° C., such as a temperature ranging from 700 to 800° C. The catalyst can be used in alcohol dehydration, olefin cracking, MTO processes, and alkylation of aromatics by alcohols with olefins and/or alcohols.

Abstract: The present invention concerns an additive for reducing the formation of coke and/or carbon monoxide in thermal hydrocarbon cracking units and/or of other organic compounds in heat exchangers. The additive according to the invention is essentially composed of diethyl disulphide (DEDS) or dipropyl disulphide(s) (DPDS) or dibutyl disulphide(s) (DBDS) and can be used on the metal walls of a cracking reactor and on the metal walls of a heat exchanger placed downstream from the cracking reactor, and during the process of cracking hydrocarbons and/or other organic compounds.

Abstract: The invention provides a method for producing methanol and its products exclusively from a geothermal source as the sole source material also using the needed energy from the geothermal energy source. The method includes separating or isolating carbon dioxide accompanying hot water or steam of the source, generating hydrogen from the water and subsequently preparing methanol from the carbon dioxide and hydrogen. The methanol can be further converted into dimethyl ether or other products.

Abstract: Ethylene separation processes are described herein. The ethylene separation processes generally include introducing a feed stream including ethylene and butene into a de-ethenizer; and separating the ethylene from the butene via fractional distillation within the de-ethenizer to form an overhead stream including separated ethylene and a bottoms stream including separated butene, wherein the de-ethenizer operates at a pressure of less than 350 psig.

Abstract: A new family of crystalline aluminosilicate zeolites has been synthesized that has been designated UZM-43. These zeolites are similar to previously known ERS-10, SSZ-47 and RUB-35 zeolites but are characterized by unique x-ray diffraction patterns and compositions and have catalytic properties for carrying out various hydrocarbon conversion processes. Catalysts made from these zeolites are useful in hydrocarbon conversion reactions.

Abstract: The process and apparatus converts ethylene in a dilute ethylene stream that may be derived from an FCC product to heavier hydrocarbons. The catalyst may be an amorphous silica-alumina base with a Group VIII and/or VIB metal. The catalyst is resistant to feed impurities such as hydrogen sulfide, carbon oxides, hydrogen and ammonia. At least 40 wt-% of the ethylene in the dilute ethylene stream can be converted to heavier hydrocarbons.

Abstract: The process and apparatus converts ethylene in a dilute ethylene stream that may be derived from an FCC product to heavier hydrocarbons. The catalyst may be an amorphous silica-alumina base with a Group VIII and/or VIB metal. The catalyst is resistant to feed impurities such as hydrogen sulfide, carbon oxides, hydrogen and ammonia. At least 40 wt-% of the ethylene in the dilute ethylene stream can be converted to heavier hydrocarbons.

Abstract: A process and catalyst for improving the yield of propylene from residual oil feedstock includes obtaining residual oil feedstock from a vacuum distillation tower. The residual oil feedstock has contaminant metals such as sodium or vanadium. The residual oil feedstock is contacted with a cracking catalyst in a catalytic cracking zone to make products. A ZSM-5 zeolite, a binder, a filler and a metal trap are components of the cracking catalyst. The metal trap has a trapping agent in an outer shell of the catalyst, a trapping agent in the ZSM-5 binder or combinations thereof. After reacting, the cracking catalyst is separated from the products in a separator zone, then regenerated by combusting coke deposited on a surface of the cracking catalyst in an oxygen-containing environment. The cracking catalyst is returned to the catalytic cracking zone. The catalyst with the metal trap is also disclosed.

Abstract: Systems and methods are provided herein for cooling an olefin cracking reactor effluent stream. One provided method includes reacting a hydrocarbon feedstock including C4+ olefins in an olefin cracking reactor to produce an olefin cracking reactor effluent stream, providing the olefin cracking reactor effluent stream to an inlet of a contact cooler, contacting the olefin cracking reactor effluent stream with a first quench liquid in a first contact zone in the contact cooler to produce a first bottoms stream and an intermediate vapor stream, contacting the intermediate vapor stream with a second quench liquid in a second contact zone in the contact cooler to produce a second bottoms stream and a cooled vapor stream, and removing the cooled vapor stream from an outlet of the contact cooler. The method can also include cooling the first bottoms stream to provide a cooled first bottoms stream, and cooling the second bottoms stream to provide a cooled second bottoms stream.

Abstract: Distillate cracks to propylene more readily than VGO. Additionally, less branched hydrocarbons crack to propylene more readily than more branched hydrocarbons. Oligomerization to diesel range oligomers followed by catalytic cracking with less branched oligomers can provide more propylene.

Abstract: One exemplary embodiment can be a process for fluid catalytic cracking. The process can include providing a first feed including one or more heavy hydrocarbons to a riser of a riser-reactor, and obtaining a second feed from an oligomerization zone. Usually, the second feed includes one or more light alkene oligomeric hydrocarbons and is provided downstream from the first feed for producing propene.

Abstract: Manufacture of propylene and ethylene in a FCC unit. Each FCC riser comprises an acceleration zone, a lift stream feed nozzle, a main hydrocarbon stock feed nozzle, and an olefinic naphtha feed nozzle. Mixed FCC catalyst comprising at least 2 percent by weight pentasil zeolite and at least 10 percent by weight Y-zeolite is injected at the bottom of each FCC riser. Olefinic naptha is injected through the olefinic feed nozzle, main hydrocarbon stock is injected through the main hydrocarbon stock feed nozzle and lift stream is injected through the lift stream feed nozzle. Lift stream comprises olefinic C4 hydrocarbon stream and optionally steam and/or a fuel gas. Olefinic C4 hydrocarbon steam is cracked in the acceleration zone at 600 to 800° C., 0.8 to 5 kg/cm2 (gauge) pressure, WHSV 0.2 to 100 hr up 1 and vapour residence time 0.2 to 5 seconds.

Abstract: Exemplary embodiments of the present invention relate to the processing of hydrocarbon-containing feedstreams in the presence of an interstitial metal hydride containing catalyst comprising a surface, and a Group VI/Group VIII metal sulfide coated onto the surface of the interstitial metal hydride. The catalysts and processes of the present invention can improve overall hydrogenation, product conversion, as well as sulfur reduction in hydrocarbon feedstreams.

Abstract: The present invention relates to a catalyst for hydrocarbon steam cracking, a method of preparing the same, and a method of preparing olefin by the hydrocarbon steam cracking by using the catalyst, and more specifically, to a catalyst for hydrocarbon steam cracking for preparing light olefin including an oxide catalyst (0.5?j?120, 1?k?50, A is transition metal, and x is a number corresponding to the atomic values of Cr, Zr, and A and values of j and k) represented by CrZrjAkOx, wherein the composite catalyst is a type that has an outer radius r2 of 0.5R to 0.96R (where R is a radius of a cracking reaction tube), a thickness (t; r2?r1) of 2 to 6 mm, and a length h of 0.5r2 to 10r2, a method of preparing the same, and a method of preparing light olefins such as ethylene, propylene, etc., by performing the hydrocarbon steam cracking reaction in the presence of the composite catalyst.

Abstract: A process for producing a catalyst additive for an FCC catalytic cracking process, the process comprising the steps of providing an MFI or MEL aluminosilicate having a silicon/aluminium atomic ratio of from 10 to 250; de-aluminating the MFI or MEL aluminosilicate by extracting from 20 to 40 wt % of the alumina therefrom; combining the de-aluminated MFI or MEL aluminosilicate with a binder; and calcining the combination of the de-aluminated MFI or MEL aluminosilicate and the binder at elevated temperature to produce the catalyst additive.

Abstract: One exemplary embodiment may be a process for fluid catalytic cracking. The process can include providing a stream through a plurality of distributors to a riser terminating in a reaction vessel. Often, the plurality of distributors includes a first distributor set having at least two distributors positioned around a perimeter of the riser, a second distributor set having at least two distributors positioned around the perimeter of the riser, and a third distributor set having at least two distributors positioned around the perimeter of the riser.

Abstract: Ruthenium and osmium carbene compounds that are stable in the presence of a variety of functional groups and can be used to catalyze olefin metathesis reactions on unstrained cyclic and acyclic olefins are disclosed. Also disclosed are methods of making the carbene compounds. The carbene compounds are of the formula where M is Os or Ru; R1 is hydrogen; R is selected from the group consisting of hydrogen, substituted or unsubstituted alkyl, and substituted or unsubstituted aryl; X and X1 are independently selected from any anionic ligand; and L and L1 are independently selected from any neutral electron donor. The ruthenium and osmium carbene compounds of the present invention may be synthesized using diazo compounds, by neutral electron donor ligand exchange, by cross metathesis, using acetylene, using cumulated olefins, and in a one-pot method using diazo compounds and neutral electron donors.