Showing papers on "Catalyst support published in 1970"

Recovery of Sulfur from Flue Gases Using a Copper Oxide Absorbent

Abstract: The body of information presented in this paper is directed to those individuals concerned with development of methods to remove SO2 from stack gases. The manuscript describes a dry, solid absorbent prepared by impregnating copper salts into a 1/16-inch alumina catalyst support. A preliminary process design and economic evaluation for power plant utilization are included. Previous pilot-scale and economic studies of an SO2 removal process using a mixed metal oxide, alkalized alumina, identified major disadvantages of the absorbent. They were rapid degradation of the solid, excessive consumption of reducing gas, and high temperature difference between absorption and regeneration steps. Thermodynamic calculations and commercial availability of a strong alumina catalyst support suggested that the disadvantages would be minimized for an absorbent prepared by impregnation of copper salts into the support. A number of such absorbents were prepared and their properties determined experimentally. Absorption of SO...

Carbon monoxide conversion catalysts

Abstract: This invention relates to a catalyst, to a process for the manufacture thereof and to a process for manufacturing hydrogen by reacting carbon monoxide with water at 150* - 550*C in the presence of the above catalyst. This catalyst comprises an active phase consisting of the mixed oxides of (a) copper and (b) a trivalent metal selected from aluminum, chromium, manganese, iron and cobalt, at least 60 percent by weight of said mixed oxides having a spinel structure. The catalyst is manufactured by admixing the catalyst components in solution with a heatdecomposable complexing organic compound or with a heatdecomposable gel-forming compound, the solvent being evaporated thereafter and the mixture being finally roasted at a temperature of at least 200*C.

Hydrocarbon conversion catalyst and process

Abstract: A hydrocarbon conversion catalyst comprising an inert support combined with an active catalytic complex comprising either SbF5-HF or SbF5-HSO3F. The catalyst is particularly suitable for isomerization, alkylation and polymerization processes.

Raney mixed catalyst

Abstract: A Raney mixed catalyst for use as a fuel cell electrode. The catalyst contains nickel, iron and one of the metals titanium or zirconium. The catalyst is prepared from a Raney alloy, which contains aluminum as the inactive component. The alloy is in at least one or two homogeneous quaternary phases.

Preparation of structures with a coating of al2o3/sio2 fibers bonded to al2o3 for use as catalyst substrates

Abstract: A REFRACTORY COMPOSITION SUITABLE AS A CATALYST SUPPORT COMPRISING A POROUS COATING OF AL2O3/SIO2 FIBERS SURROUNDING AND INTEGRALLY BONDED TO AN INNER PORTION COMPRISING AL2O3.

Catalytic process including continuous catalyst injection without catalyst removal

Abstract: THE HYDRODESULFURIZATION OF A CRUDE OIL OR A REDUCED CRUDE CONTAINING THE ASPHALTENE FRACTION PROCEEDS AT UNEXPECTEDLY LOW TEMPERATURES BY UTILIZING A CATALYST COMPRISING A GROUP VI AND GROUP VIII METAL ON ALUMINA WHEREIN THE CATALYST PARTICLES ARE VERY SMALL AND HAVE A DIAMETER BETWEEN ABOUT 1/20 AND 1/40 INCHES, AND THE FEED IS PASSED IN DOWNFLOW OPERATION OVER A FIXED BED OF THE CATALYST. THE LOW TEMPERATURE ADVANTAGE DEPENDS UPON HIGH HYDROGEN PRESSURE AND THE PROCESS IS PRESSURE DROPLIMITED RATHER THAN CATALYST ACTIVITY LIMITED. THE PRESENT INVENTION PRESENTS A TWO PRONGED ATTACK ON PRESSURE DROP. FIRST, PLUGGING AT THE TOP OF THE CATALYST BED AND COINCIDENT INCREASE IN PRESSURE DROP IS PREVENTED BY STARTING THE REACTION WITH ONLY A PORTION OF THE TOTAL CATALYST REQUIRED FOR A FULL CYCLE AND INJECTING FRESH CATALYST TO THE TOP OF THE CATALYST BED WHILE THE REACTION IS IN PROGRESS WITHOUT REMOVING ANY CATALYST FROM THE PROCESS. FURTHERMORE, DISREGARDING PLUGGING, PRESSURE DROP DUE TO THE SMALL PARTICLE SIZE OF THE CATALYST IS RETARDED SINCE THE TOTAL CATALYST LOAD IS NOT INTRODUCED UNTIL THE CATALYST CYCLE IS NEAR AN END. IN THIS MANNER, THE SAMLLEST AMOUNT OF CATALYST IS PRESENT WHEN THE CATALYST IS MOST ACTIVE AND THE GREATEST AMOUNT OF CATALYST IS NOT PRESENT UNTIL THE CATALYST IS LEAST ACTIVE. THIS INVENTION CAN BE APPLIED TO OTHER FIXED BED PROCESSES WHEREIN FOULING AT THE TOP OF THE BED OR PRESSURE DROP REPRESENTS A PROCESS LIMITATION AND WHEREIN FRESHLY INJECTED CATALYST CAN PERFORM AS A FILTERING MEDIUM IN ADDITION TO PREFORMING A CATALYTIC FUNCTION.

High surface area nickel catalyst

Abstract: A STABILIZED HIGH SURFACE AREA NICKEL CATALYST WHICH IS PARTICULARLY USEFUL FOR REMOVING TRACE QUANITIES OF OXYGEN FROM INERT GASES IS DESCRIBED. THE NICKEL-SILICA CATALYST HAS A NICKEL SURFACE AREA GREATER THAN 70 M.2/G. AND A TOTAL SURFACE AREA IN THE RANGE OF ABOUT 225 M.2/G. TO ABOUT 300 M.2/G. THE ACTIVE CATALYST CONTAINS FROM ABOUT 25 WT. PERCENT TO ABOVE 50 WT. PERCENT NICKEL AND OF ITS TOTAL SILICA CONTENT 30 TO 90 WT. PERCENT IS DERIVED FROM PRECIPITATED SILICATE IONS.

Low density alumina spheres of improved strength at high temperature

Abstract: Low density alumina spheres of improved strength at high temperature are prepared by commingling an acidic alumina sol and an aqueous rare earth metal salt solution with an ammonia precursor at below gelation temperature and dispersing the mixture as droplets in a hot oil bath. The hydrogel spheres which form are aged, washed and dried, and calcined. Low density alumina spheres are useful as a catalyst or as a catalyst support, particularly in the conversion of hot exhaust gases from an internal combustion engine.

Sulfide precipitated catalysts

Abstract: A SUPPORTED METAL SULFIDE CATALYST PREPARED BY IMPREGNATING A POROUS SOLID CATALYST SUPPORT WITH AN AQUEOUS SOLUTION OF A SALT OF A HYDROGENATION METAL COMPONENT SELECTED FROM THE GROUP CONSISTING OF MOLYBDENUM, TUNGSTEN, IRON GROUP METALS, AND MIXTURES THEREOF, PRECIPITATING THE RESPECTIVE METAL SULFIDES AND SUBSEQUENTLY DRYING IN AN INERT ATMOSPHERE POSSESSES IMPROVED HYDROGENATION, DENITRIFICATION AND DESULFURIZATION ACTIVITY.

Reforming with a platinum-tin-iridium catalyst

Abstract: Reforming a naphtha in the presence of hydrogen with a catalyst composition comprising a porous solid carrier, 0.01 to 3 weight percent platinum, 0.01 to 5 weight percent tin; and 0.001 to 1 weight percent iridium; also the novel supported platinum-tin-iridium catalyst.

Method of catalyst preparation

Abstract: A PROCESS FOR THE PREPARATION OF SUPPORTED CATALYSTS. THE COMPONENTS OF THE CATALYST ARE MELTED AND MIXED WITH A SUITABLE POROUS SUPPORT MATERIAL OR CARRIER. ON COOLING, THE SUPPORT MATERIAL IS COATED AND/OR IMPREGNATED WITH THE SOLIDIFIED CATALYST.

Extruded alumina catalyst support and the preparation thereof

Abstract: A METHOD OF PREPARING EXTRUDED, GEL-TYPE ALUMINA CATALYST SUPPORTS IS DISCLOSED. THE METHOD INVOLVES MIXING CRYSTALLINE ALUMIN HYDRATE AND ABOUT 2 TO ABOUT 25 PARTS BY WEIGHT OF FINELY DIVIDED, LOW DENSITY POLYETHYLENE PER 100 PARTS OF ALUMINA AND AN EXTRUDABLE AMOUNT OF WATER, EXTRODING THE MIXTURE AND CALCINING THE MIXTURE IN A MOLECULAR OXYGEN-CONTAINING GAS TO SUBSTANTIALLY BURN AWAY THE POLYETHYLENE AND FORM A SUPPORT. ADDITIONALLY ABOUT 0.5 TO 3 WEIGHT PERCENT OF STARCH AND/OR METHYL CELLULOSE MAY BE INCLUDED IN THE MIXTURE PRIOR TO EXTRUSION AND CALCINATION. THESE LATTER MATERIALS ARE ALSO BURNED OUT OF THE SUPPORT DURING THE CALCINATION.

Infra-red spectra of acetylene on γ-alumina and γ-alumina-supported platinum, and effect of sulphur compounds

Abstract: The i.-r. spectra of the surface species formed by the initial adsorption of acetylene on γ-alumina and γ-alumina-supported-platinum were obtained at room temperature. The adsorption of acetylene on γ-alumina resulted in weak and strong adsorbent-adsorbate interactions. The bands at 3260, 2697, 2680, 2665, 2640, 2167 and 1945 cm–1 were due to weakly held acetylene. The bands at 3305 and 2000 cm–1 were due to strongly held acetylene on the γ-alumina surface. The adsorption of acetylene on supported platinum resulted in a sharp band at 1690 cm–1. Hydrogenation of acetylene adsorbed on the γ-alumina surface was greatly facilitated by the presence of platinum. Addition of H2S and COS to the system resulted in poisoning of the adsorbents due to the dissociation of these sulphur compounds and the subsequent formation of (Al2O3)·Sx and PtSx complexes. Poisoning substantially reduced acetylene adsorption on the γ-alumina and platinum. There was no evidence to show the adsorption of acetylene on poisoned sites. This system illustrated that both the catalyst and the catalyst support are susceptible to sulphur poisoning.

Ethynylation catalyst catalyst preparation and process

Abstract: PARTICULATE CATALYST, CONSISTING ESSENTIALLY OF CUPROUS ACETYLIDE COMPLEXES CONTAINING AT LEAST 1.75 CARBON ATOMS PER COPPER ATOM, AND HAVING A TOTAL SURFACE AREA OF AT LEAST 5.0 SQUARE METERS PER GRAM, ARE PREPARED AT 50120*C. BY THE SIMULTANEOUS ACTION OF FORMALDEHYDE AND ACETYLENE AT A PARTIAL PRESSURE OF LESS THAN 2.0 ATMOSPHERES ON CUPRIC COMPOUNDS SLURRIED IN SUBSTANTIALLY NEUTRAL AQUEOUS MEDIA AND USED TO CATALYZE ETHYNYLATION IN A CONTINOUS STIRRED REACTION AT 60-120*C. AND ACETYLENE PARTIAL PRESSURES BELOW 2.0 ATMOSPHERES.

Barium promoted iron oxide for use as a catalyst in steam-iron process for producing hydrogen

Abstract: Barium is incorporated with iron oxide to prepare a catalyst or contact mass for use in steam-iron process for producing hydrogen. A process for producing hydrogen using such catalyst is set forth.

Dehydrogenating propane over chromia-alumina catalyst

Abstract: Triethyl aluminum is employed as reactant in a conversion to valuable products, forming an alumina by-product consisting predominantly of alumina alpha-monohydrate and a significant amount of amorphous alumina. Particles of this by-product are marketed as a technical grade of boehmite. A precursor mixture is prepared comprising calcined alumina powder, a larger amount of said technical grade of boehmite, and an aqueous solution containing ammonium dichromate. Said mixture is extruded, sliced into pellets, calcined in steam, and cooled to provide dehydrogenation catalyst consisting of about 20 percent chromia and 80 percent alumina. Propane at subatmospheric pressure is dehydrogenated at a high conversion per pass to provide an attractive yield of propene over said catalyst at 570*-680* C. at a space velocity of from about 0.2 to about 5 volumes of liquid propane per volume of catalyst per hour during a commercially acceptable catalyst life.

Hydrofining-hydrocracking process using palladium-containing catalyst

Abstract: A HYDROFINING-HYDROCRACKING PROCESS WHICH COMPRISES CONTACTING A HYDROCARBON FEED CONTAINING MORE THAN 50 PARTS PER MILLION OF ORGANIC NITROGEN AND CONTAINING SUBSTANTIAL AMOUNTS OF MATERIALS BOILING ABOVE 200* F., SAID FEED BEING SELECTED FROM THE GROUP CONSISTING OF PETROLEUM DISTILLATES, SOLVENT-DEASPHALTED PETROLEUM RESIDUA, SHALE OILS AND COAL TAR DISTALLATES, IN A REACTION ZONE WITH HYDROGEN AND A CATALYST, AT HYDROFINING-HYDROCRACKING CONDITIONS INCLUDING A TEMPERATURE IN THE RANGE 400* TO 950* F., A PRESSURE IN THE RANGE 800 TO 3500 P.S.I.G., A LIQUID HOURLY SPACE VELOCITY IN THE RANGE 0.1 TO 5.0, AND A TOTAL HYDROFGEN SUPPLY RATE OF 200 TO 20.000 S.D.F. OF HYDROGEN PER BARREL OF FEEDSTOCK, REMOVING AMMONIA FROM THE EFFLUENT FROM SAID REACTION ZONE, AND RECOVERING HYDROFINED AND HYDROCRACKED PRODUCTS FROM SAID REACTION ZONE, SAID CATALYST COMPRISING: (A) A GEL MATRIX COMPRISING: (A) AT LEAST 15 WEIGHT PERCENT SILICA, (B) ALUMINA, IN AN AMOUNT PROVIDING AN ALUMINATO-SILICA WEIGHT RATIO OF 15/85 TO 80/20, (C) NICKEL OR COBALT, OR THE COMBINATION THEREOF, IN THE FORM OF METAL, OXIDE, SULFIDE OR ANY COMBINATION THEREOF, IN AN AMOUNT OF 1 TO 10 WEIGHT PERCENT, BASED ON SAID MATRIX, CALCULATED AS METAL, (D) MOLYBDENUM OR TUNGSTEN, OR THE COMBINATION THEREOF, IN THE FORM OF METAL, OXIDE, SULFIDE OR ANY COMBINATION THEREOF, IN AN AMOUNT OF 5 TO 25 WEIGHT PERCENT, BASED ON SAID MATRIX, CALCULATED AS METAL; (B) A CRYSTALLINE ZEOLITIC MOLECULAR SIEVE: (A) CONTAINING FROM 0.1 TO 2.0 WEIGHT PERCENT PALLADIUM, CALCULATED AS METAL, (B) CONTAINING LESS THAN 5 WEIGHT PERCENT SODIUM, (C) BEING IN PARTICULATE FORM AND BEING DISPERSED THROUGHOUT SAID MATRIX BY COGELATION OF SAID MATRIX AROUND SAID SIEVE; SAID CATALYST COMPOSITE BEING FURTHER CHARACTERIZED BY IN AVERAGE PORE DIAMETER BELOW 100 ANGTROMS AND A SURFACE AREA ABOVE 200 SQUARE METERS PER GRAM.

Zinc-containing zeolite catalyst

Abstract: A CRYSTALINE ALUMINO-SILICATE ZEOLITE CATALYST SUPPORT HAVING HIGH CRYSTALLINE STABILITY AND ACIDIC CATALYTIC ACTIVITY IS PREPARED FROM AN ALKALI ZEOLITE, PREFERABLY A Y-FAUJASITE, BY (1) REMOVING THE ALKALI METAL IONS TO BELOW ABOUT 1.0% W. BY ION EXCHANGE, AND (2) INCORPORATING ZINC IONS AND CALCINING AT A HIGH TEMPERATURE OF ABOUT 800*C. THE SUPPORT CAN THEN BE COMBINED WITH HYDROGENATIVE METALS SUCH AS GROUP VIII AND GROUP VI-B, FOLLOWED BY DRYING AND CALCINING TO PROVIDE SUPERIOR HYDROISOMERIZATION AND HYDROCRACKING CATALYSTS.

Polymerization of epoxides with dialkylaluminum acetylacetonate catalyst systems

Abstract: Catalyst systems for the polymerization of epichlorohydrin, propylene oxide, and allyl glycidyl ether have been prepared from pure, separately synthesized dialkylaluminum acetylacetonates (R2Alacac). Adding small amounts of water to R2Alacac gives a catalyst system with enhanced activity. An even more active catalyst system for yielding high molecular weight, epichlorohydrin-containing polymers is obtained when another organometallic compound is added to the R2Alacac-0.5 water components. The R2Alacac-0.5 water-R2Zn system has been studied in detail. Variation in the molar proportion of water and structural changes in the chelate structure of the R2Alacac component have been examined. Results indicate that the bis-chelate structure, acac(R)-Al-O-Al(R)acac, plays a major role in catalyst formation. A bimetallic catalyst species containing aluminum and zinc atoms is proposed, with zinc functioning primarily in monomer coordianation and with aluminum involved primarily in polymer chain growth.

Halide addition and distribution in the reactivation of platinum-rhenium catalysts

Abstract: There is disclosed a method for reactivating a fixed bed of used platinum group metal-alumina catalyst of the type in which the alumina is derived from hydrous alumina predominating in alumina trihydrate. Such catalysts are employed in, for instance, the catalytic reforming of gasoline boiling range hydrocarbons to obtain fuels of high-octane ratings or aromatics. The method for reactivating the catalyst which has declined in activity during use and contains carbonaceous deposits, involves treating the deactivated catalyst at elevated temperatures with an oxygencontaining gas to burn the carbonaceous deposits therefrom. The relatively carbon-free catalyst is contacted under controlled conditions with a gaseous stream containing small amounts of chlorine, in combined or elemental form, oxygen and often water vapor to deposit chloride in a first portion of the catalyst bed. After the chlorine component is added to the catalyst, preferably in a relatively short period of time, the catalyst is then contacted with a gaseous stream containing oxygen and water vapor. This treatment may continue for a longer time than the chlorine treating period and until the chloride deposited on the catalyst is distributed through a major portion of the catalyst bed. Distribution of the chloride is a function of the time, temperature and water vapor partial pressure observed during the treatment and thus the distribution is controlled essentially by kinetics. The extent of water contact with the catalyst is limited by controlling the amount of water in the gaseous streams and the length of the overall treatment.

Olefin conversion process using catalyst containing a metal phosphate support

Abstract: OLEFINS ARE C ONVERTED INTO OTHER OLEFINS HAVING DIFFERENT NUMBERS OF CARBON ATOMS BY CONTACT WITH A CATALYST ACTIVE FOR DISPROPORTIONATING PROPYLENE INTO ETHYLENE AND BUTENE AND COMPRISING A PHOSPHATE OF ALUMINUM, ZIRCONIUM, CALCIUM, MAGNESIUM OR TITANIUM AND PROMOTED BY ONE OR MORE SELECTED COMPOUNDS OF TUNGSTEN, MOLYBDENUM, OR RHENIUM.

Modified al-nn catalyst for dimerizing olefins

Abstract: THIS INVENTION RELATES TO THE MANUFACTURE OF A DIMERIZATION CATALYST, TO THE CATALYST THUS OBTAINED AND TO A PROCESS FOR DIMERZING OLEFINS WITH THE SAID CATALYST. THE CATALYST IS MANUFACTURE BY REACTING A DIHYDROCARBYL ALUMINUM MONOHALIDE WITH A CONTROLLED AMOUNT OF WATER AT A TEMPERATURE LESS THAN 20*C., THEN SEPARATING THE INSOLUBLE FRACTION AND THEREAFTER CONTACTING THE SOLUBLE FRACTION WITH NICKEL OR A NICKEL COMPOUND. THE CATALYST ISPERFERABLY USED AT TEMPERATURES HIGHER THAN 20*C.

Catalyst for oxidation of olefins

Abstract: A CATALYST FOR OXIDATION OF OLEFINS, BASED ON BISMUTH, MOLYBDENUM AND OXYGEN, AS WELL AS SILICON, OR SILICON AND AN ALKALI METAL, OR SILICON AND BORON, OR SILICON, AN ALKALI METAL AND BARON, THE EMPIRICAL FORMULA OF THE CATALYST BEING BI2SIBM0CMDBCOF WHERE M IS AN ALKALI METAL; A=5-20 B=0.02-1 C=12 D=0-2.3 E=0.0.1 F=43-72 THE CATALYST MAY ALSO COMPRISE A CARRIER WITH THE SPECIFIC SURFACE OF 0.3-3 M.20G. IN AN AMOUNT OF 20-90% OF THE TOTAL WEIGHT OF THE CATALYST.

The Effect of Catalyst Support on the Decomposition of Methane to Hydrogen and Carbon

Abstract: Decomposition of methane into carbon and hydrogen over Cu/Ni supported catalysts was investigated. The catalytic activities and the lifetimes of the catalysts were studied. Cu/Ni supported on TiO2 showed high activity and long lifetime for the reaction. Transmission electron microscopy (TEM) studies revealed the relationship between the catalyst activity and the formation of the filamentous carbon over the catalyst after methane decomposition. While different types of filamentous carbon formed on the various Cu/Ni supported catalysts, an attractive carbon nanotubes was observed in the Cu/Ni supported on TiO2. Key Words: Methane decomposition, carbon nanotube, Cu/Ni supported catalysts.

Catalyst for nitrogen oxide reduction

Abstract: A CATALYST FOR REDUCING NITROGEN OXIDES IN AN AUTOMOBILE EXHAUST GAS STREAM COMPRISING ACTIVATED ALUMINA PELLETS CONTAINING UP TO ABOUT 10 MOLE PERCENT ZINC OXIDE.

Stabilized amorphous silica-alumina catalytic cracking catalysts

Abstract: There is provided a method for improving the attrition resistance and heat stability of a silica-alumina fluid catalytic cracking catalyst where the catalyst contains up to 35 weight percent alumina by treating the catalyst with steam such that the catalysts stability factor is increased to a value of at least 12.5. The above treatment provides an improved fluid catalytic cracking catalyst for utilization for the cracking of a hydrocarbon charge under the catalytic cracking conditions.

Catalyst for hydrazine decomposition and the method of producing the catalyst

Abstract: A catalyst is provided for decomposing hydrazine base monopropellants and providing multiple hydrazine-ignition restarts. The catalyst comprises a carrier material selected from the group consisting of high area ceramics, and 1/2 to 8% of active iridium, ruthenium, or mixtures thereof, based on the total weight of the catalyst. The active metal is deposited primarily on the exterior surface of the carrier. A second metal catalyst can be contained primarily within the interior of the carrier. The method of producing the catalyst comprises impregnating the carrier with an alcohol solution containing a salt of iridium, ruthenium, or a mixture thereof, to deposit the metal on the exterior surface only of the carrier. The precious metal is reduced to an active pure metal by contact with a fluid reducing agent selected from the group consisting of hydrogen and hydrogen-inert gas mixtures. A second metal catalyst can be deposited uniformly throughout the catalyst by impregnating the carrier with an aqueous solution containing a compound of the second metal catalyst.