Showing papers on "Catalyst support published in 1986"

Recent basic research in hydrodesulfurization catalysis

Abstract: Article de synthese sur les catalyseurs Co-Mo/Al 2 O 3 et Ni-Mo/Al 2 O 3 d'hydrodesulfuration: techniques d'investigation, identification des structures actives et sites actifs, influence du support (alumine, silice, carbone), comprehension du comportement catalytique

Ethylene oxide catalyst and process for preparing the catalyst

Abstract: This invention relates to an ethylene oxide catalyst having an improved selectivity which catalyst comprises silver, a promoting amount of alkali metal, a promoting amount of rhenium and a promoting amount of rhenium co-promotor selected from sulfur, molbydenum, tungsten, chromium and mixtures thereof supported on a porous refractory support.

Mixed alcohols production from syngas

Abstract: Mixed alcohols are produced from carbon monoxide and hydrogen gases using an easily prepared catalyst/co-catalyst metal catalyst. The catalyst metals are molybdenum, tungsten or rhenium. The co-catalyst metals are cobalt, nickel or iron. The catalyst is promoted with a Fischer-Tropsch promoter like an alkali or alkaline earth series metal or a smaller amount of thorium and is further treated by sulfiding. The composition of the mixed alcohols fraction can be selected by selecting the extent of intimate contact among the catalytic components.

Aromatization of Hydrocarbons over Platinum Alkaline Earth Zeolites

Abstract: A new platinum/zeolite catalyst is more active and selective for the aromatization of paraffins, especially hexanes and heptanes, than are the platinum/alumina naphtha reforming catalysts presently used in petroleum refining. The new catalyst, which contains highly dispersed platinum clusters in barium-exchanged potassium Zeolite L, is also effective for alkylcyclopentane aromatization. The preparation and characterization of the Pt/BaKL-zeolite catalyst are described. Its catalytic performance and the reactions it catalyzes are compared with those of other platinum reforming catalysts. Unlike the conventional reforming catalysts, which utilize acidic sites of the support as well as platinum sites, the Pt/BaKL catalyst is nonacidic and catalyzes aromatization using only the catalytic properties of the platinum clusters. The catalyst is extremely sensitive to poisoning by sulfur, but its stability for reforming of thoroughly desulfurized feed is illustrated by an uninterrupted one-year run with a refinery light naphtha.

Catalyst compositions and methods of making the same

Abstract: A method of making a catalyst composition comprising an activated alumina coating stabilized against thermal degradation includes applying a coating of alumina having one or more platinum group metal catalytic components dispersed thereon onto a carrier substrate and calcining the coating. The calcined coating is then impregnated with a solution of a thermal stabilizer-precursor and calcined again to provide a thermal stabilizer in the alumina. Bulk ceria, optionally an aluminum-stabilized bulk ceria, may also be added to the composition, preferably at specified minimum levels, including a high purity bulk ceria on which one or more non-rhodium platinum group metal catalytic components, e.g., platinum, optionally, are dispersed. A separate aspect of the invention provides for a method of making a catalyst composition including dispersing one or more platinum group metal catalytic components on an activated alumina and calcining the combined alumina and platinum group metal catalytic components. The steps are carried out under limited acidification conditions whereby at least minimum dispersions of the platinum group metal catalytic components are attained. The invention also provides for catalyst compositions resulting from either or both the foregoing methods.

Method of producing high-strength high surface area catalyst supports

Abstract: A catalyst support having both substantial high strength and high surface area can be produced by heating a shaped mixture of a porous oxide having a surface area of at least 20 m 2 /g and the precursor of an inorganic binder for the porous oxide. The binders are precursors of alumina, silica, or titania, and are capable of imparting substantial strength to the support at relatively low firing temperatures.

Hydrosilylation catalyst, method for making and use

Abstract: A colloidal hydrosilylation catalyst is provided by effecting reaction between a silicon hydride or a siloxane hydride and a Pt(O) or Pt(II) catalyst. The colloidal catalyst forms stable mixtures with olefinically unsaturated organopolysiloxanes.

Hydrogenation of a hydrocrackate using a hydrofinishing catalyst comprising palladium

Abstract: An improved nickel-tin hydrogenation catalyst additionally comprising palladium provides a highly active catalyst more easily activated than conventional nickel hydrogenation catalysts, and a process employing the improved catalyst to stabilize lubricating oils to ultraviolet radiation is disclosed.

Preparation of monolithic catalyst supports having an integrated high surface area phase

Abstract: A method of preparing a monolithic catalyst support having an integrated high surface area phase is provided. A plasticized batch of ceramic matrix material intimately mixed with high surface area powder is formed into the desired shape for the monolith and then heated to sinter the ceramic. The resulting monolith has a strong substrate of the ceramic matrix material and a high surface area phase provided by the high surface area powder extruded with the batch.

Activated cobalt catalyst and synthesis gas conversion using same

Abstract: Synthesis gas comprising carbon monoxide and hydrogen is converted to a liquid hydrocarbon by contacting the synthesis gas under conversion conditions with a catalyst prepared by subjecting a cobalt carbonyl-impregnated alumina or silica support to an activation procedure at a temperature not exceeding 500° C. comprising, in sequence, (A) reduction in hydrogen, (B) oxidation in an oxygen-containing gas, and (C) reduction in hydrogen.

Single riser fluidized catalytic cracking process utilizing a C3-4 paraffin-rich co-feed and mixed catalyst system

Abstract: There is provided a catalytic cracking operation featuring a single riser reaction zone having a lower and an upper section wherein a variety of hydrocarbon conversion reactions takes place, a stripping zone in which entrained hydrocarbon material is removed from catalyst and a regeneration zone in which spent cracking catalyst is regenerated, which comprises: (a) cracking a C3-4 paraffin-rich feed in the lower section of the riser reaction zone in the presence of the second component of a mixed catalyst system, the second component being zeolite Beta and/or a shape selective medium pore crystalline silicate zeolite, to provide light olefins and conversion products of light olefins including aromatics and hydrogen; and, (b) cracking a heavy hydrocarbon feed in an upper section of the riser reaction zone in the presence of the first component of the mixed catalyst system, the first component being an amorphous cracking catalyst and/or a large pore crystalline cracking catalyst, to provide gasoline boiling range components, there being a sufficient difference between one or more physical characteristics of the catalyst components as to permit particles of second catalyst component to remain in the lower section of the riser reaction zone for a longer average period of time than particles of first catalyst component and, optionally, to permit particles of first catalyst component to be separated from particles of second catalyst component in the stripping zone.

Monolithic catalyst support and catalyst deposited on the support

Abstract: A monolithic catalyst support for use in the purification of exhaust gases comprises: a metal substrate; an oxide membrane formed on the surface of the substrate by applying heat treatment to the substrate; and an active alumina layer formed on the oxide membrane, wherein the composition of the metal substrate is composed of from 5 to 30% by weight of chromium (Cr), from 1 to 10% by weight of aluminum (Al), from 0.1 to 0.5 by weight of one or more of potassium (K), rubidium (Rb), cesium (Cs), francium (Fr), calcium (Ca), strontium (Sr), barium (Ba), radium (Ra) and lanthanoid elements and the balance of iron (Fe). The endurance of the monolithic catalyst can be improved because incorporation of the lanthanoid elements can improve the purifying performance.

Preparation of monolithic catalyst support structures having an integrated high surface area phase

Abstract: A method of forming a monolithic ceramic catalyst support having a high surface area phase of porous oxide embedded within the monolith structure is provided. The porous oxide phase is incorporated into a sinterable ceramic structure as a discrete discontinuous phase. The high surface area necessary for effective catalyst support is thereby provided within the ceramic structure, which is sintered to provide appreciable density and strength.

Novel catalyst and process for hydrogenation of unsaturated hydrocarbons

Abstract: Dienes and/or acetylene impurities in an olefin feed; in particular a propylene feed, may be selectively hydrogenated in a single stage by use of a catalyst of palladium supported on alumina which is substantially crystalline alpha alumina, wherein the average pore radius is 200-2000 Å, with at least 80% of the pores having a pore radius within the range of 100 to 3000 Å. The surface acidity of the catalyst is generally from 0.002 to 0.05 millimole of pyridine absorbed per gram of catalyst. The active palladium surface area is from 20 to 200 m2 /g. The palladium is in the form of crystallines having an average size of at least 25 Å.

High temperature stable catalyst and process for preparing same

Abstract: The disclosure is concerned with a high temperature stable catalyst comprising an alumina base support and a catalytically active component supported on the support. The support is featured by its specific composite oxide having a specific surface area of at least 10 m 2 /g and a structural form of amorphous state or a phase resemble to lanthanoide β-alumina. The composite oxide can be converted to lanthanoide β-alumina when heated to an elevated temperature above 1000° C. within 2 hours. The composite oxide is substantially free from such ingredients as accelerate grain growth of alumina. The ingredients are for example Cr, Sr or Ce. The present disclosure is also concerned with a process for preparing the catalyst and a process for conducting chemical reactions such as steam reforming, desulfurization of heavy oil, cracking of hydrocarbons, etc. using the catalyst.

Sulphided platinum group metal-silicalite dehydrogenation catalysts

Abstract: Alkanes are dehydrogenated to alkenes, for example n-butane to n-butenes by contact with a catalyst comprising a silicalite and a platinum group metal the catalyst being substantially free of alkali and alkaline earth metals. The selectivity of the product to butenes is improved by either presulphiding the catalyst or by passing a minor amount of a sulphur-containing compound with the alkane feed. The catalyst can be prepared by either forming the silicalite in the presence of the platinum group metal or alternatively contacting preformed silicalite with a solution of a platinum group metal.

Catalyst for conversion of synthesis gas to diesel fuel and process for preparation of such catalyst

Abstract: A catalyst for the conversion of synthesis gas comprising cobalt on a high surface area, high purity, low acidity alumina support of gamma-alumina, eta-alumina or mixtures thereof, whereby the catalyst is prepared by (A) impregnation of the alumina support with a non-aqueous, organic solvent impregnation solution of cobalt nitrate containing sufficient amounts of a Group IIIB or IVB metal salt to provide said catalyst with from about 0.05 to about 100 parts by weight of a Group IIIB or IVB metal oxide per 100 parts by weight cobalt, (B) reduction of the impregnated alumina support by heating, in the presence of hydrogen, at a heating rate of from about 0.5° to about 5° C. per minute to a maximum temperature in the range of 180° to about 220° C. for a hold time of 6 to about 24 hours and thereafter heating the impregnated alumina support in the presence of hydrogen while heating up to a maximum hold temperature of from about 250° to about 400° C. for a hold time of 6 to about 65 hours.

Hydroprocessing conditions affect catalyst shape selection

Abstract: Diffusion characteristics, pressure drop limitations, catalyst pore size, catalyst loading techniques, and catalytic activity requirements all affect the selection of the catalyst shape used in hydroprocessing of heavy distillates Haldor Topsoe Inc has studied the effects of these hydroprocessing conditions on various shapes of its TK-551 nickel-molybdenum hydroprocessing catalysts The studies were carried out using Arabian Heavy vacuum gas oil (VGO) For hydroprocessing heavy distillates, polylobed catalysts and dense loading techniques have obvious advantages The higher external surface of polylobed catalysts ensures better accessibility to the inner surface of the catalyst, and dense loading allows more catalytic activity in a given reactor volume However there are drawbacks Polylobed catalysts tend to pack less densely thus reducing volume activity And dense loading results in higher pressure through the bed The philosophy behind the use of polylobed catalysts is to improve the diffusion characteristics

Chapter 11 Supported Bimetallic Catalysts Prepared by Controlled Surface Reactions

Abstract: Publisher Summary This chapter discusses the supported bimetallic catalysts prepared by controlled surface reactions (CSRs). It is demonstrated that the principle of controlled surface reactions is a powerful approach, and supported bimetallic catalysts prepared by these methods possess unique catalytic properties, in hydrocarbon conversion and in hydrogenation of different organic compounds. Catalysts prepared in this way possess unique catalytic properties. Different supported bimetallic catalysts can be prepared by means of CSRs: the catalysts with direct metal–metal interaction and the catalysts in which the second metal is strongly bound to the support. The properties of these catalysts strongly depended on (1) the type of surface reactions used during the preparation and (2) the thermal treatment applied before the reaction. The chapter emphasizes the mode of controlling the reactions. The chemical nature of the alumina-supported platinum catalyst is used as a driving force to obtain surface entities with direct metal-metal interactions. This approach is based on the reactivity of hydrogen preadsorbed on metal surfaces.