Abstract: An improved catalytic process for heavy hydrocarbon conversion (usually but not necessarily in the presence of nickel and vanadium in the feedstock and on the catalyst) to produce lighter and selective molecular weight fractions. This process is specifically targeted as a means of retaining specialty high-valued, preferably microspherical additives (SHVA) which assist in attaining preferred conversion products such as gasoline, especially the recent gasolines meeting compositional requirements of "Reformulated Fuel".Selective magnetic retention of these high-cost specialty additives can be achieved by incorporating into them selective magnetic moieties, preferably manganese, the heavy rare earths and superparamagnetic iron. Selective retention is achieved by passing spent or regenerated catalyst containing small amounts of these SHVAs through a magnetic separator, and selectively recycling them back to the circulating catalyst.

Abstract: Zeolite cracking catalyst compositions and additives that contain a Lewis acid supported on alumina are useful to process hydrocarbon feedstocks. The compositions are especially useful for the production of reduced sulfur gasoline.

Abstract: A process for the fluid catalytic cracking of heavy fraction oils containing heavy metals such as Ni and V, which comprises withdrawing a portion of ferrite-containing catalyst particles circulating in a fluid catalytic cracking apparatus, separating the thus withdrawn catalyst particles into metals-richly deposited catalyst particles and metals-poorly deposited ones by using a magnetic separator and then returning the metals-poorly deposited catalyst particles, together with fresh ferrite-containing catalyst particles, into said cracking apparatus.

Abstract: Treatment of sulphur bearing hydrocarbons, especially olefin feedstocks to the oxo process, with a nickel-containing catalyst, especially spent hydrogenation catalyst, which may be amine treated.

Abstract: Middle distillates can be produced efficiently in high yields by catalytically cracking petroleum hydrocarbons by contacting the petroleum hydrocarbons at cracking conditions with a catalyst composition comprising a cation-exchanged stevensite.

Abstract: Rare earth oxides, such as Nd.sub.2 O.sub.3 disperse onto the surface of SiO.sub.2 /Al.sub.2 O.sub.3 and act as weakly basic titrants. This lowers the acidity of SiO.sub.2 /Al.sub.2 O.sub.3 to close to that of chlorided alumina, as shown by model compound reaction tests. This support also disperses a noble metal such as Pt much better than undoped SiO.sub.2 /Al.sub.2 O.sub.3 and similar to chlorided alumina. Platinum on the rare earth modified silica alumina can function as a hydrocarbon conversion catalyst in reactions where Pt/chlorided Al.sub.2 O.sub.3 is used, such as in reforming, and isomerization, especially wax isomerization.

Abstract: By continuously or intermittently adding amounts of magnetically active moieties, e.g. iron compounds, over time so that the moiety deposits on a catalyst or sorbent in a fluid catalytic cracker or similar circulating hydrocarbon conversion unit, older catalyst, being more magnetic, can be readily separated from catalyst which has been in the system a shorter time. Separation is readily accomplished by passing the catalyst and/or sorbent through a magnetic field and discarding the more magnetic 50% by wt. or more preferably 20% by wt., while recycling the remainder back to the hydrocarbon conversion unit.

Abstract: A process is provided for effecting catalytic conversion of an organic compound-containing feedstock to conversion product which comprises contacting said feedstock under catalytic conversion conditions with a catalyst comprising an active form of a functionalized inorganic, porous, non-layered crystalline phase having uniformly sized pores of at least about 13, e.g., at least about 15, Angstrom Units in diameter.

Abstract: A process is provided for effecting catalytic conversion of an organic compound-containing feedstock to conversion product which comprises contacting said feedstock under catalytic conversion conditions with a catalyst comprising an active form of an inorganic, porous crystalline phase exhibiting, after calcination, a hexagonal arrangement of uniformly-sized pores having diameters of at least about 13, e.g., at least about 15, Angstrom Units and exhibiting a hexagonal electron diffraction pattern that can be indexed with a d.sub.100 value greater than about 18 Angstrom Units.

Abstract: A demetallization process for catalysts used for chemical conversion of hydrocarbons, the catalysts containing at least vanadium as a metal poison, wherein the poisoned catalyst is contacted in a sulfiding zone with a sulfiding agent and a hydrocarbon having a minimum boiling point of about 300.degree. F., the hydrocarbon being at least partially vaporizable at the temperature in the sulfiding zone.

Abstract: Disclosed is a method for cracking a hydrocarbon material. The method includes introducing a stream including a hydrocarbon fluid and a carrier fluid into a reaction zone. A microwave discharge plasma is continuously maintained within the reaction zone, and in the presence of the hydrocarbon fluid and the carrier fluid. Reaction products of the microwave discharge are collected downstream of the reaction zone.

Abstract: By continuously or intermittently adding amounts of magnetically active moieties, e.g. iron compounds, over time so that the moiety deposits on a catalyst or sorbent in a fluid catalytic cracker or similar circulating hydrocarbon conversion unit, older catalyst, being more magnetic, can be readily separated from catalyst which has been in the system a shorter time. Separation is readily accomplished by passing the catalyst and/or sorbent through a magnetic field and discarding the more magnetic 50% by wt. or more preferably 20% by wt., while recycling the remainder back to the hydrocarbon conversion unit.

Abstract: This invention concerns a process for reducing a refining catalyst before it is put into use, the catalyst containing a support and an active phase based on at least one noble or non-noble metal of group VIII or of group Ib of the periodic classification of elements, consisting of:(a) impregnating the catalyst with an aqueous or organic solution of a reducing agent,(b) decomposing the reducing agent by heating with a catalyst, and(c) drying the catalyst thus obtained.The catalyst is used in selective hydrogention of a feed such as olefin, acetylenes, diolefins etc.

Abstract: A process is disclosed wherein a regenerator is operated in an incomplete mode of combustion to regenerate FCC catalyst to burn coke contained thereon in the presence of a CO oxidation promoter. The quantity of the CO oxidation promoter is regulated so that there is at least two and preferably at least three times the minimum quantity of CO oxidation promoter present than necessary to prevent temperature excursions in the dilute phase caused by afterburn combustion of CO to CO.sub.2. The regeneration zone is maintained in an incomplete mode of combustion defined by having a CO content greater than 1.0 percent and preferably from 1 to 10 percent.

Abstract: Disclosed is a method for cracking a hydrocarbon material. The method includes introducing a stream including a hydrocarbon fluid into a reaction zone. A microwave discharge plasma is continuously maintained within the reaction zone, and in the presence of the hydrocarbon fluid. Reaction products of the microwave discharge are collected downstream of the reaction zone.

Abstract: In a process for the liquefaction of coal under increased pressure and temperature in a liquefaction zone, it is recommended that the liquefaction product exiting the liquefaction zone is fed into a coking area, there cooling the gases and vapors produced, (which are mainly distillate oil vapors), preferably in direct heat exchange with the coal paste. The gases and vapors not condensed during this heat exchange are extracted from the unit as end products. The proposed type of process partially transfers oil production from the liquefaction zone to the coking zone, so that the liquefaction zone can be operated with low pressure. In addition, due to the direct heat exchange of the product vapors with the fresh coal paste, a great part of the exothermic heat created by the liquefaction reactions can be fed back into the process.

Abstract: A crystalline zeolite SSZ-24 is prepared using an adamantane quaternary ion as a template.

Abstract: A process for the catalytic cracking of heavy petroleum fractions into lower hydrocarbons, such as fuel products. The process comprises contacting the petroleum fractions at an elevated temperature with a cracking catalyst comprising (a) a layered metal oxide of the titanometallate type intercalated with an interspathic polymeric chalcogenide, e.g., polymeric silica and, optionally (b) a porous crystalline silicate component such as a large pore zeolite material.

Abstract: Catalytic dewaxing of wax containing hydrocarbon feedstocks is undertaken in the presence of a catalyst composition comprising a dehydrogenation metal in combination with a non-acidic microporous crystalline material containing tin to maximize liquid yield.

Abstract: Catalytic cracking catalysts and their use in catalytic cracking processes are disclosed. The instant catalytic cracking catalysts are useful for cracking a hydrocarbon feedstock to produce lower boiling hydrocarbons. The catalysts comprise an effective amount of at least one non-zeolitic molecular sieve characterized in its calcined form by an adsorption of isobutane of at least 2 percent by weight at a partial pressure of 500 torr and a temperature of 20.degree. C. The non-zeolitic molecular sieve is characterized as containing framework tetrahedral components of aluminum and phosphorus and at least one additional framework tetrahedral component, e.g., the non-zeolitic molecular sieve may be a silicoaluminophosphate as described in U.S. Pat. No. 4,440,871.

Abstract: A process for the hydrogenation of heavy oils, residual oils, waste oils, used oils, shell oils, and tar sand oils by hydrogenating a slurry of the oil at a partial hydrogen pressure of 50-300 bar, a temperature of 250.degree.-500.degree. C., a space velocity of 0.1-5 T/m.sup.3 h, and a gas/liquid ratio of 100-10000 Nm.sup.3/ T, wherein the additive comprises two different grain size portions, a fine grain portion having a grain size of 90 microns or less and a coarse grain portion having a grain size of 100-1000 microns.

Abstract: Sulfur oxides are removed at least partially from the gaseous regenerator effluent of a fluid catalytic cracking unit operated with feedstock containing sulfur compounds and converted to hydrogen sulfide in the cracking zone by associating sulfur oxides in the gas with at least one rare earth compound, preferably cerium or a rare earth mixture rich in cerium, supported on discrete particles of alumina. The alumina particles may be a component of particles of a composite fluid cracking catalyst or separate fluidizable entities other than cracking catalyst and physically admixed with the catalyst particles.

Abstract: A process is disclosed for the catalytic dewaxing of a hydrocarbon oil by contacting said oil at catalytic dewaxing conditions with a catalyst comprising a crystalline aluminum silicate which has the following composition in terms of the molar ratios of the oxides:(0.9+0.2)Z.sub.p O.sub.q :Al.sub.2 O.sub.3 :xSiO.sub.2 : yH.sub.2 Owherein Z is at least one cation, p and q are each at least one and satisfy the electroneutrality of Z.sub.p O.sub.q, x is at least 10 and y/x is 0-25, and which crystalline aluminum silicate has a defined characteristic X-ray diffraction pattern as set forth in Table A.

Abstract: Hydrocracking catalysts comprise a Group VIB and/or non-noble metal Group VIII hydrogenation component in conjunction with an LZ-210 zeolite preferably of SiO.sub.2 :Al.sub.2 O.sub.3 greater than 9.0, which zeolite has been hydrothermally treated and ammonium ion-exchanged. In a preferred embodiment, the zeolite is essentially free of rare earth metals, and most preferably, essentially free of all metals except the Group VIB or non-noble Group VIII.

Abstract: An novel class of iron-aluminum-phosphorus-silicon-oxide molecular sieves is disclosed which contain as framework constituents FeO.sub.2.sup.-, and/or FeO.sub.2.sup.-2, AlO.sub.2.sup.-, PO.sub.2.sup.+ and SiO.sub.2 tetrahedral oxide units. These compositions are prepared hydrothermally, preferably using organic templating agents and are suitably employed as adsorbents and catalysts.

Abstract: The acidity of a zeolite catalyst is reduced by calcination in an essentially water-free atmosphere at temperatures above 700.degree. C., preferably from 725.degree. to 800.degree. C., to reduce the alpha value to less than about 10 percent of its original value. The low acidity catalysts produced in this way may be used for conversions requiring low acidity, shape selective catalysis, including dewaxing. The calcined, low acidity catalysts exhibit improved dewaxing activity.

Abstract: The invention concerns a hydrocarbon cracking catalyst containing a mixture of amorphous matrix with a zeolite, the zeolite having a SiO.sub.2 /Al.sub.2 O.sub.3 molar ratio ranging from about 8 to 70, a sodium content lower than 0.15% by weight, a parameter a.sub..degree. of elementary mesh from 24.55 to 24.24.times.10.sup.-10 m, a capacity C.sub.Na to retake sodium ions, expressed in grams of sodium per 100 grams of modified zeolite, higher than 0.85, a specific surface higher than 400 m.sup.2.g.sup.-1, a sodium ion uptake steam adsorption capacity at 25.degree. C. (with a P/Po ratio of 0.10) higher than 6% by weight, a pore distribution such that from 1 to 20% of the pore volume is pores of a diameter ranging from 20 to 80.10.sup.-10 m, the remaining pore volume being essentially pores of a diameter lower than 20.10.sup.-10 m, the matrix being characterized by the following textural properties:S .gtoreq.100 m.sup.2.g.sup.-1TPV .gtoreq.0.4 cm.sup.3.g.sup.-1PV.sub.75 .gtoreq.0.25 cm.sup.3.g.sup.-1PV.sub.

Abstract: A process for regenerating a spent, naturally occurring catalyst characterized by an iron content of about 10 to 70 wt. % as metal comprises contacting the spent catalyst with a mixture of water vapor and air in a water vapor/air ratio of between 1:1 to 20:1 at a flow rate of about 0.1 to 50 l/min., a temperature of about 200.degree. to 700.degree. C., a pressure of about 0.3 to 80 atmospheres for a time of about 0.1 to 20 hours so as to obtain a regenerated catalyst having a crystallinity value of about 1.0 to 6.5.

Abstract: A cobalt-molybdenum catalyst and a method for preparing same, said catalyst useful for the hydrodesulfurization (HDS) and hydrodenitrogenation (HDN) of distillates of petroleum. The catalyst is supported by aluminum phosphate or an aluminum borate. In a preferred embodiment the catalyst has a low cobalt content, between 0.5% and 2.0% by weight calculated as CoO, and a molybdenum content of between 10% and 20% by weight, calculated as MoO.sub.3. The phosphorus or boron compounds added to the aluminum before the impregnation of the active metals prevents the formation of undesirable compounds of the CoAl.sub.2 O.sub.4 type, which is inactive in HDS. It is for that reason that the catalyst has a formulation with 70% less cobalt than the previous state-of-the-art catalysts. Very small crystals, highly dispersed on the surface of the catalyst, whose formula is CoMoO.sub.4, are responsible for the stability and the high level of activity in HDS and HDN which results.

Abstract: This invention provides a novel base-exchanged shape-selective hydrogenation-dehydrogenation-dehydrocyclization catalyst composition which is a zeolite matrix having a silica-alumina ratio of at least 12, and having a shape-selective functioning intrazeolitic Group VIII metal content between about 0.01-10 weight percent.The zeolite catalyst is adapted for efficient shape-selective metal function hydrogenolysis, dehydrogenation and aromatization conversion of hydrocarbon mixtures, with a minimized acid-catalyzed cracking activity.

Abstract: A process for converting heavy hydrocarbon into light hydrocarbon which comprises contacting heavy hydrocarbon having an API gravity at 25.degree. C. of less than about 20, such as Boscan heavy crude oil and tar sand bitumen, with a liquid comprising water, and carbon monoxide in the presence of an externally added catalyst comprising a mixture of sulfur and at least one of ferric oxide, ferric sulfide, ferrous sulfide and pyrite a residue and a phase comprising light hydrocarbon, gas and water; separating the residue and said phase; and recovering from said phase light hydrocarbon having an API gravity at 25.degree. C. of greater than about 20, and having a hydrogen to carbon mole ratio greater than that of the heavy hydrocarbon feedstock.

Abstract: A fluid coking process is provided in which a catalyst comprising an alkaline earth metal ferrite is present in the fluid coking zone.

Abstract: Vacuum distillation residue oil having a Conradson carbon value of 5 to 40% and a specific gravity of 0.9 to 1.10 is thermally cracked in the presence of iron ore particles in fluidized state in a thermal cracking reactor thereby to produce light oils and cracked gases and to form by-product carbon, which is caused to deposit on the iron ore particles, which are then transferred to and heated at 800.degree. C. to 1200.degree. C. in a reducing furnace to be reduced in a solid state reaction, into sponge iron. Thus, heavy oil is thermally cracked and sponge iron is produced by an economical, integrated process.

Abstract: Sulfur oxides are removed from flue gas in a catalyst regenerator in a fluid catalyst cracking system while liquid-hydrocarbon product yield from the system is maintained at a high level by heating a nonzeolitic, silica-containing catalyst to 800.degree.-1500.degree. F.; impregnating 0.1 to 25 weight percent aluminum onto the catalyst particles; and cycling the resulting particles through the cracking reactor and catalyst regenerator in the cracking system, the impregnated catalyst being particularly adaptable for cracking heavy, metals-containing feeds such as residua.

Abstract: A catalyst is described for use in a process for oxidizing and/or cracking a heavy hydrocarbon under fluidizing conditions in the presence of the catalyst, including simultaneously or subsequently reducing iron oxides in said catalyst and then reacting the reduced oxidation-state iron with steam to produce hydrogen, said catalyst consisting essentially of from 30 to 60 wt % Fe, 0.1 to 10 wt % Ni, and 10 wt % or less SiO.sub.2, and having a specific surface area of from 0.1 to 30 m.sup.2 /g and an apparent specific gravity of from 2.5 to 4.0.

Abstract: A process for processing a sulfur-containing heavy oil, which comprises:in a first zone, catalytically cracking a sulfur-containing heavy oil in the presence of fluidized catalyst particles containing about 30 to 60 wt % Fe to thereby convert the heavy oil to a light oil, deposit sulfur-containing coke on the catalyst particles, and partially fixing the decomposed sulfur compounds with the reduced iron contained in the catalyst particles as iron sulfide;in a second zone, contacting the catalyst from the first zone with an oxygen containing gas in an amount less than that theoretically required to thereby partially combust the coke on the catalyst, reduce the iron in the catalyst, and fix the sulfur compounds contained in the coke as iron sulfide; andin a third zone, contacting the reduced catalyst from the second zone with steam in a fluidized manner to produce hydrogen and hydrogen sulfide and to convert the reduced iron and iron sulfide in the catalyst to iron oxides, with the iron oxide-containing catalyst

Abstract: A catalyst for the steam dealkylation of aromatic hydrocarbons, comprising a carrier and 3 metals, is regenerated in the reaction zone containing the catalyst bed, after disconnection of said zone from the producing unit, by proceeding to the successive steps of: scavenging said zone with hydrogen and then with an inert gas, progressively replacing said inert gas by a gas containing molecular oxygen, burning the catalyst at a temperature lower than 650.degree. C. so as to calcine the carbon deposits of the catalyst, passing through the catalyst bed an air stream containing halogen to increase the halogen content of the catalyst, calcining by means of an air stream at a temperature of 300.degree.-600.degree. C. and purging with an inert gas before reconnecting said reaction zone to the producing unit.

Abstract: A novel catalyst precursor which comprises a Group IV-B transition metal oxide deposited on the surface of an inorganic metal oxide support, preferably alumina; especially where the Group IV-B transition metal oxide is deposited on the support surface as discrete areas separated by areas of support surface which contain little, if any, of said Group IV-B transition metal oxide; and a catalyst composition comprised of a cluster of a Group IV-B transition metal oxide and a Group VIII metal preferably a Group VIII noble metal, deposited on an inorganic metal oxide support, particularly an alumina support, especially where the clusters are deposited on the surface of the support, as discrete clusters separated by areas of support surface which contain little, if any, of said Group VI-B transition metal oxide, or clusters of said Group IV-B and Group VIII metals.

Abstract: Novel crystalline silicates which in dehydrated form have the composition in terms of moles of the oxides: (1.0.+-.0.3)(R).sub.2/n O.[aFe.sub.2 O.sub.3.bAl.sub.2 O.sub.3.cGa.sub.2 O.sub.3.y(dSiO.sub.2.eGeO.sub.2)], wherein R is one or more mono- or bivalent cations and a, b, c, d, e, y and n are as defined hereinafter are disclosed. The thermally stable silicates are suitably employed as extracting agents, drying agents, ion exchange agents, catalysts and catalyst carriers.

Abstract: A process for producing a cracked distillate and hydrogen from a heavy oil which comprises cracking the heavy oil in the presence of laterite or a laterite-containing catalyst while simultaneously depositing coke on said laterite or laterite-containing catalysts, reducing the laterite or laterite-containing catalyst on which the coke is deposited, and forming a hydrogen-rich gas by contacting the reduced laterite or laterite-containing catalyst with steam.

Abstract: Catalytic process for steam dealkylation of a charge containing at least one alkyl aromatic hydrocarbon, such as a charge issued from effluents of units for catalytic reforming or for producing aromatic hydrocarbons, wherein the catalyst contains an alumina carrier, from 0.1 to 1% of rhodium, from 0.05 to 1% of TiO.sub.2 and optionally from 0.1 to 1% of ruthenium, palladium, iridium, platinum or osmium and/or from 0.01 to 5% of lithium, sodium, potassium, rubidium or cesium.

Abstract: Carbon monoxide and sulfur oxides are removed from catalyst regenerator flue gas in an FCC system using a nonzeolitic cracking catalyst and sulfur from the flue gas is shifted to form hydrogen sulfide, which is recovered in the gases removed from the cracking reactor in the system by reacting carbon monoxide in the regenerator flue gas with oxygen in contact with a particulate carbon monoxide combustion promoter, reacting sulfur oxides in the regenerator flue gas with particulate alumina physically mixed with the nonzeolitic catalyst to form a sulfur-containing solid, and forming hydrogen sulfide in the cracking reactor by contacting the sulfur-containing solid with the hydrocarbon feed.

Abstract: Carbon monoxide and sulfur oxides are removed from flue gas produced in a catalyst regenerator in an FCC system and sulfur from the flue gas is shifted to form hydrogen sulfide, which is recovered in the gases removed from the cracking reactor in the system by introducing sufficient molecular oxygen into the catalyst regenerator to provide an atmosphere therein having a molecular oxygen concentration of at least 0.1 volume percent, reacting carbon monoxide in the regenerator flue gas with oxygen in contact with a particulate carbon monoxide combustion promoter physically admixed with the cracking catalyst, reacting sulfur oxides in the regenerator flue gas with silica-free alumina included as a discrete phase in the FCC catalyst to form a sulfur-containing solid in the catalyst, and forming hydrogen sulfide in the cracking reactor by contacting the sulfur-containing solid with the hydrocarbon feed.

Abstract: Alkylaromatic hydrocarbons are steam-dealkylated in the presence of a catalyst comprising an alumina carrier and 0.1 to 2% b.w. of a group VIII noble metal, 0.05 to 2% of a group I.sub.B metal and 0.01 to 5% of an alkali metal.

Abstract: Process for steam dealkylation of alkylaromatic hydrocarbons, particularly useful to produce benzene from toluene and to de-alkylate the alkylaromatic hydrocarbons contained in the effluents from catalytic reforming and aromatic production units, wherein the catalyst contains, in addition to an alumina carrier (a) at least one metal selected from ruthenium, rhodium, palladium, osmium, iridium and platinum (b) rhenium and (c) an alkali metal selected from lithium, sodium, potassium, rubidium and cesium.

Abstract: The amount of NO.sub.x formed during regeneration of a cracking catalyst in the presence of a metallic carbon monoxide combustion catalyst is decreased without substantially adversely affecting the carbon monoxide combustion activity of the promoter by subjecting the combustion-promoting catalyst to steam treatment prior to employing it in the cracking catalyst regeneration operation.

Abstract: The preparation of an ultra-stable, high surface area alpha-alumina catalyst and catalyst support suitable for use in high temperature processes such as petroleum refining processes, e.g., resid cat cracking and steam reforming, is disclosed. The process comprises impregnating high surface area gamma-alumina having narrow pores with a carbonaceous material that readily chars to form carbon. The impregnated alumina is then heated to a temperature sufficient to induce charring, following which the gamma-alumina is converted to alpha-alumina by further heating. The carbon is subsequently removed by oxidation. The alpha-alumina thus produced can withstand temperatures up to at least about 1000.degree. C. in the presence of steam without substantial loss of surface area.

Abstract: Prevention of detrimental effect of metals such as nickel, vanadium and iron on the activity of a cracking catalyst when used in a cracking process having essentially no hydrogen added thereto is achieved by using in the cracking process novel cracking catalyst having less than 40 weight percent zeolite content and including antimony metal or a compound of antimony prior to subjecting the cracking catalyst to hydrocarbon cracking conditions.

Abstract: Used cracking catalyst fines from a cracking process wherein antimony or a compound thereof is used as a metals passivation agent are used as an efficient passivation agent in a cracking process.

Abstract: By continuously or intermittently adding amounts of magnetically active moieties, e.g. iron compounds, over time so that the moiety deposits on a catalyst or sorbent in a fluid catalytic cracker or similar circulating hydrocarbon conversion unit, older catalyst, being more magnetic, can be readily separated from catalyst which has been in the system a shorter time. Separation is readily accomplished by passing the catalyst and/or sorbent through a magnetic field and discarding the more magnetic 50% by wt. or more preferably 20% by wt., while recycling the remainder back to the hydrocarbon conversion unit.