US3759823A - Hydrocarbon conversion with platinum second metal catalysts in proportions which form ordered alloys - Google Patents

Hydrocarbon conversion with platinum second metal catalysts in proportions which form ordered alloys Download PDF

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US3759823A
US3759823A US00129439A US3759823DA US3759823A US 3759823 A US3759823 A US 3759823A US 00129439 A US00129439 A US 00129439A US 3759823D A US3759823D A US 3759823DA US 3759823 A US3759823 A US 3759823A
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platinum
metal
catalysts
catalyst
atomic
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E Davies
J Elkins
R Pitkethly
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BP PLC
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BP PLC
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/321—Catalytic processes
    • C07C5/324—Catalytic processes with metals
    • C07C5/325—Catalytic processes with metals of the platinum group
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/373—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen with simultaneous isomerisation
    • C07C5/393—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen with simultaneous isomerisation with cyclisation to an aromatic six-membered ring, e.g. dehydrogenation of n-hexane to benzene
    • C07C5/41—Catalytic processes
    • C07C5/415—Catalytic processes with metals
    • C07C5/417—Catalytic processes with metals of the platinum group
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used
    • C10G35/085—Catalytic reforming characterised by the catalyst used containing platinum group metals or compounds thereof
    • C10G35/09—Bimetallic catalysts in which at least one of the metals is a platinum group metal

Definitions

  • a hydrocarbon conversion catalyst of 0.01-% wt. metal on a refractory support contains platinum and a second metal which forms a solid solution with Pt, the atomic amounts of each being equivalent to amounts forming ordered alloy structures.
  • the second metal may be Co, Ni, Fe, Cu, Sn, Pd (particularly these six), Ir, Rh, Ag, Au, Bi, Hg, Sb, Pd or Cd and preferably there is at least 45 atomic percent Pt.
  • the catalysts may be prepared by known impregnation or ion-exchange techniques and are preferably reduced before use at 250-600 C.
  • the preferred use is dehydrocyclisation or dehydrogenation of C -C hydrocarbons, particularly the catalytic reforming of -204 C. boiling range petroleum fractions.
  • a catalyst suitable for the conversion of hydrocarbons comprising from 0.01 to 10% wt. of metal on a refractory support is characterised in that it contains platinum and a second metal which forms asolid solution with platinum, the atomic amounts of the platinum and the second metal being substantially equivalent to amounts which form ordered alloy structures.
  • platinum alloys The metallurgy of platinum alloys is well established and metals known to form solid solutions with platinum include cobalt, nickel, iron, copper, tin, palladium, iridium, rhodium, silver, gold, bismuth, mercury, antimony, lead, and cadmium.
  • ordered structures In accordance with established metallurgical principles the existence of ordered structures in any bi-metallic system can be readily determined, and many of them are already known. These ordered structures have atomic proportions of the two metals in a simple ratio. The ratios may vary with diiferent metals but for any two metals there will be relatively few ordered structures, usually 5 at the most. The most common are AB i.e. atomic percent A, 50 atomic percent B A B i.e.
  • This invention relates to platinum-containing catalysts and their use for the catalytic conversion of hydrocarbons.
  • Catalysts of platinum on a refractory support are well known.
  • the platinum which may be present in an amount of 0.1 to 5% wt., has good activity for hydrogenation or dehydrogenation and dehydrocyclisation depending on the process conditions.
  • additional functions of e.g. isomerisation and cracking can be given to the catalyst.
  • substantially equivalent to amounts which form ordered alloy structures means i 5 atomic percent for each metal.
  • the platinum is substantially equal to or greater than the amount of the other metal.
  • the platinum is preferably thus at least 45 atomic percent.
  • the preferred second metals are cobalt, nickel, iron, copper, tin and palladium.
  • the support may be contacted simultaneously with solutions containing ions of platinum and the second metal or sequentially in either order.
  • the contacting is carried out sequentially with the platinum containing solution being used first.
  • the platinum and the second metal may be added by ion-exchange, this being a known term indicating that the ions combine chemically with active sites on the surface of the support. Particularly in the case of supports having few or weak active sites, the support should be washed exhaustively with water while the ions are still in a water-soluble state until the wash water is free of metal ions. This washing ensures that the only metal remaining on the support is in ion-exchanged form.
  • the platinum and the second metal ions can be added in either cation or anion form, the former being preferred since the most commonly used supports are cation-exchangers.
  • the platinum and the second metal may also be added by impregnation in conventional manner and this is, in fact, preferred.
  • metal ions includes complex ions where the metal is attached to a ligand, particularly water, ammonium, or halogen.
  • complex ions are the usual form of ions for many metals in aqueous or ammoniacal solution.
  • platinum containing solutions used in catalyst preparations are tetrammine platinous chloride giving tetrammine platinous cations and chloroplatinic acid giving hexachloroplatinate anions.
  • the second metal solution may contain any suitable salt, e.g. chloride, nitrate, or acetate and may again be an ammoniacal solution.
  • the conditions of the contacting with platinum and the second metal ions the temperature, time and concentration of ion in solutionwill depend on the ease of uptake and the desired uptake, and may be readily determined by experiment if necessary. Suitable conditions have been found to include temperatures of -110" C., times of 1 to 72 hours and solution concentrations of 0.001 to 2 molar.
  • the washing to remove uncombined ions desirably uses de-ionised water and, as indicated above, is continued until the wash water is free of ions of platinum and the second metal.
  • the temperature may also be 10 to 110 C., and the time 1 to 72 hours using, preferably, 2 to 100 ml. of water/ml. of catalyst.
  • the refractory support is preferably an inorganic oxide of an element of Groups II, III and IV of the Periodic Table, a mixture of two or more such oxides or a compound containing one or more of such oxides in its empirical formula.
  • Preferred individual oxides are silica or alumina
  • preferred mixed oxides are silica-alumina, silica-magnesia, or boria-alumina
  • preferred minerals are alumina-silicates e.g. zeolites.
  • the catalysts may also contain from 0.1 to 8% wt. of halogen, particularly chlorine.
  • the catalyst may be dried e.g. at 50-110 C. for 1 to 24 hours, and calcined at 250 to 600 C. for 1 to 24 hours. Desirably the catalysts are also reduced before use by heating them in a reducing atmosphere at 200 to 600 C. for 1 to 24 hours.
  • the reducing atmosphere is preferably a flowing stream of hydrogen.
  • the reduction of the dual-metal catalyst may be more difficult than that of catalysts containing only platinum and care should be exercised to ensure reduction. The extent of reduction can be monitored by hydrogen uptake from a closed system in which hydrogen is circulated over the catalyst.
  • the present invention includes a process for the catalytic conversion of hydrocarbons comprising contacting the hydrocarbons under conversion conditions with a catalyst containing platinum and a second metal on a refractory support having a composition as previously described.
  • Conversion conditions can vary widely depending on the feedstock and reaction but they are normally within the ranges Temperature C 0-600 Pressure p.s.i.g 0-3000 Space velocity v./v./hr 0.1-20' Hydrogemhydrocarbon mole ratio 0-20z1
  • the preferred hydrocarbon feedstocks may be derived from any convenient source e.g. from petroleum and their precise nature will depend on the reaction required.
  • the preferred hydrocarbons are parafiins and/ or olefins and/or naphthenes, particularly those having from 3 to 25 carbon atoms.
  • the preferred dehydrogenation or dehydro cyclisation reactions may be operated under the following ranges of conditions:
  • the catalysts of the present invention may be used for the catalytic reforming of hydrocarbons boiling in the gasoline range 15 to 204 C.), particularly petroleum fractions, to increase the aromatic content and/ or octane number.
  • the preferred support for such use is alumina, possibly containing from 0.1 to 8% wt. of halogen, such a support having the moderate isomerisation and cracking activity usually considered desirable in catalytic reforming.
  • the feedstocks may be unsaturated hydrocarbons e.g. acetylenes, olefins, or aromatics, particularly those having'from 2 to 20 carbon atoms.
  • the process conditions may be chosen from:
  • the catalyst support is preferably relatively inert and may be for example silica, sepiolite or low-acidity alumina.
  • EXAMPLE 1 A series of platinum-copper catalysts was prepared.
  • the support used was silica of 30-60 B.S.S. mesh obtained from Hopkins and Williams Ltd. having a surface area of 170 m. g. It was freed from iron impurities by washing with normal HCl and distilled water.
  • a catalyst containing 1.8% wt. platinum was prepared by contacting g. silica with 9.22 ml. of a molar solution of tetrammine platinous chloride at 25 C. for 2 h. The silica was then washed with 50 ml. aliquots of deionised water at 25 C. The final wash water was free of platinum ions.
  • the catalyst was dried at C. for 24 hours.
  • a series of platinum and copper catalysts was prepared by progressively reducing the concentration of tetrammine platinous chloride in the solution and contacting the Pt- SiO with solutions of cupric chloride in 0.880 S.G. aqueous ammonia of progressively increasing concentration. The relative concentrations were adjusted so that each catalyst had the same gram atom metal content as the 1.8% wt. Pt. on silica but varying atomic ratios of Pt and Cu, 90:10, 80:20, 70:30 and so on. In the final catalyst the contacting with platinum was omitted altogether giving a catalyst of 0.59% wt. copper on silica.
  • Example 1 feedstock and process conditions of Example 1 (ie Each catalyst was dried at 110 C. for 24 hours and 500 C., atmospheric pressure, 4000 v./v./hr. of feedstock reduced in 4000 v./v./hr. of hydrogen at 500 C. for having a 10:1 H m-hexane mole ratio).
  • the catalysts contain-
  • the platinum-tin-alumina catalysts showed the following 40 atomic percent or less of platinum had relatively ing results for rate of benzene formation low activities but the curves still show a non-linear elfect Rate of nz a i n in this region, including a definite peak in the Pt-Co curve. be ens form to Percent Pt: millimoles minr gram- EXAMPLE 4 5 100 0.13
  • a series of platinum-nickel-alumina and platinum-iron- 90 '296 alumina catalysts were prepared using the same technique 80 0'219 as in Example 3 but using nickel chloride (NiCl or iron 70 0'267 chloride (FeCl in place of cobalt chloride.
  • the catalysts 1Q were tested for dehydrocyclisation activity again using the feedstock and process conditions of Example 3. The results Again with these catalysts, variations throughout the are shown in Tables 4 and 5 below. range are seen.
  • Examples 2-5 with 100 atomic percent Pt the relative EXAMPLE 5 improvement by the incorporation of a second metal in a 5'? proportion equivalent to an ordered alloy structure is A series of platinum-palladium-alumina catalysts and a 0 series of platinum-tin-alumina catalysts (over the range 100 atomic percent Pt 100 100-50 atomic percent Pt) were prepared by the Same 70% Pt 30% Cu (Pt Cu) 15S technique as in Example 3 but using PdCl and SnCl in Pt 20% Co (Pt Co) 140 place of cobalt chloride. The catalysts were tested for 50% Pt 50% Ni (PtNi) 155 dehydrocyclisation activity again using the feedstock and 60 80% Pt 20% Fe (Pt Fe) 145 process conditions of Example 3.
  • a process for the catalytic conversion of hydrocarbons comprising contacting the hydrocarbons at a temperature of to 600 C., a pressure of 0 to 3000 p.s.i.g., a space velocity of 0.1 to 20 v./v./hr. and a hydrogenzhydrocarbon mole ratio of 0 to 20:1 with a catalyst comprisin from 0.01 to wt.
  • said catalyst containing platinum and a second metal which forms a solid solution with platinum, said second metal being selected from the group consisting of cobalt, nickel, iron, copper, tin, palladium, iridium, rhodium, silver, gold, bismuth, mercury, antimony, lead and cadmium, the atomic amount of platinum in said solid solution being at least atomic percent and being also within :5 atomic percent of the atomic amount of platinum required to form an ordered alloy structure with said second metal, and the atomic amount of said second metal in said solid solution being within :5 atomic percent of the atomic amount of said second metal required to form said ordered alloy structure with the platinum.
  • a process as claimed in claim 1 which is the dehydrogenation or dehydrocyclisation of hydrocarbons having from 3 to 25 carbon atoms at a temperature of 300 to 600 C. a pressure of 0 to 1000 p.s.i.g., a space velocity of 0.1 to 10 v./v./hr. and a hydrogen: hydrocarbon mole ratio of 0 to 20:1.
  • a process as claimed in claim 2 which is the catalytic reforming of a petroleum fraction boiling in the range 15 to 204 C.
  • the second metal is selected from the group consisting of cobalt, nickel, iron, copper, tin and palladium and wherein the platinum and the selected second metal are in atomic amounts which form any one of the following ordered alloy structures: Pt Co, PtCo; PtNi; Pt Fe, PtFe; Pt Cu, Pt Cu, PtCu; Pt Sn, Pt Sn, PtSn; P qPd, PtPd.

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US00129439A 1970-04-13 1971-03-30 Hydrocarbon conversion with platinum second metal catalysts in proportions which form ordered alloys Expired - Lifetime US3759823A (en)

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Cited By (33)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3939060A (en) * 1972-09-13 1976-02-17 Universal Oil Products Company Hydrocarbon conversion with a sulfided acidic catalytic composite
US3943053A (en) * 1974-10-04 1976-03-09 Ashland Oil, Inc. Selective hydrogenation of aromatics and olefins in hydrocarbon fractions
US3950243A (en) * 1975-03-14 1976-04-13 Universal Oil Products Company Hydrocarbon conversion with an acidic sulfur-free multimetallic catalytic composite
US3959121A (en) * 1975-05-05 1976-05-25 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic catalytic composite
US3962139A (en) * 1972-11-30 1976-06-08 Stamicarbon B.V. Catalyst preparation
US3972806A (en) * 1975-07-03 1976-08-03 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic catalyst composite
US3981795A (en) * 1975-08-08 1976-09-21 Uop Inc. Hydrocarbon conversion with an acidic multimetallic catalytic composite
US3998724A (en) * 1975-05-12 1976-12-21 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic catalytic composite
US4018668A (en) * 1975-01-16 1977-04-19 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic sulfur-free catalytic composite
US4021374A (en) * 1973-12-19 1977-05-03 Magyar Tudomanyos Akademia Szerves Kemiai Technologiai Tanszek Selective hydrogenating catalysts and a process for the preparation thereof
US4036903A (en) * 1975-08-08 1977-07-19 Uop Inc. Dehydrocyclization with an acidic multimetallic catalytic composite
US4049576A (en) * 1974-10-04 1977-09-20 Ashland Oil, Inc. Platinum-palladium catalyst for selective hydrogenation of aromatics and olefins in hydrocarbon fractions
US4065514A (en) * 1972-07-17 1977-12-27 Texaco Inc. Preparation of methane
US4115252A (en) * 1976-11-22 1978-09-19 Uop Inc. Hydrocarbon conversion with an acidic multimetallic catalytic composite
US4139570A (en) * 1976-08-27 1979-02-13 Uop Inc. Dehydrogenation of naphthene hydrocarbons
US4179406A (en) * 1976-11-22 1979-12-18 Uop Inc. Acidic multimetallic catalytic composite
US4206042A (en) * 1978-03-31 1980-06-03 Uop Inc. Hydrocarbon dehydrocyclization with an acidic multimetallic catalytic composite
US4233185A (en) * 1976-12-08 1980-11-11 Johnson, Matthey & Co., Limited Catalysts for oxidation and reduction
US4295957A (en) * 1979-04-30 1981-10-20 Exxon Research & Engineering Co. Reforming with multimetallic catalysts
US4297245A (en) * 1972-07-17 1981-10-27 Texaco Inc. Catalyst for the preparation of methane
US4384986A (en) * 1976-10-29 1983-05-24 Solvay & Cie. Particles of an alloy of noble metals with non-noble metals
US5409877A (en) * 1991-08-22 1995-04-25 Director-General Of Agency Of Industrial Science And Technology Catalyst for producing aldehyde and alcohol from olefin, carbon monoxide and hydrogen
WO1998002242A1 (en) * 1996-07-15 1998-01-22 Chevron U.S.A. Inc. Sulfur resistant hydroconversion catalyst and hydroprocessing of sulfur-containing lube feedstock
US5993644A (en) * 1996-07-16 1999-11-30 Chevron U.S.A. Inc. Base stock lube oil manufacturing process
US6462244B1 (en) * 1999-07-28 2002-10-08 Sũd-Chemie Inc. Hydrogenation catalysts
US6548447B1 (en) * 1996-01-22 2003-04-15 Regents Of The University Of Minnesota Catalytic oxidative dehydrogenation process and catalyst
WO2004105007A1 (en) * 2003-05-20 2004-12-02 Coventry University Method for making a nano-particulate medium
US20060058185A1 (en) * 2004-08-18 2006-03-16 Symyx Technologies, Inc. Platinum-copper-nickel fuel cell catalyst
US20100280295A1 (en) * 2007-09-19 2010-11-04 Max-Planck-Gesellschaft Zur Forderung Der Wissenschaften E.V. Use of a mixture of an ordered intermetallic compound and an inert material as a catalyst and corresponding hydrogenation processes
WO2012014225A2 (en) 2010-07-26 2012-02-02 Council Of Scientific & Industrial Research An improved process for the storage delivery of hydrogen using catalyst
US20130184507A1 (en) * 2006-03-15 2013-07-18 Max-Planck-Gesellschaft Zur Foerderung Der Wissenschaften E. V. Hydrogenation Process Using Catalyst Comprising Ordered Intermetallic Compound
WO2014174065A1 (en) * 2013-04-25 2014-10-30 Technical University Of Denmark Alloy catalyst material
CN112512962A (zh) * 2018-05-29 2021-03-16 株式会社斋田Fds 装置及其所使用的催化剂

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4251392A (en) * 1979-04-30 1981-02-17 Exxon Research & Engineering Co. Reforming with multimetallic catalysts
FR2466279A1 (fr) * 1979-07-02 1981-04-10 Catalyse Soc Prod Francais Nouveaux catalyseurs d'hydroreformage catalytique ou de production d'hydrocarbures aromatiques
FR2468406A1 (fr) * 1979-11-05 1981-05-08 Catalyse Soc Prod Francais Nouveaux catalyseurs de conversion d'hydrocarbures
CN114054023B (zh) * 2020-07-31 2023-08-25 中国科学院大连化学物理研究所 一种合金单原子催化剂的制备方法和应用

Cited By (45)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4297245A (en) * 1972-07-17 1981-10-27 Texaco Inc. Catalyst for the preparation of methane
US4065514A (en) * 1972-07-17 1977-12-27 Texaco Inc. Preparation of methane
US3939060A (en) * 1972-09-13 1976-02-17 Universal Oil Products Company Hydrocarbon conversion with a sulfided acidic catalytic composite
US3962139A (en) * 1972-11-30 1976-06-08 Stamicarbon B.V. Catalyst preparation
US4021374A (en) * 1973-12-19 1977-05-03 Magyar Tudomanyos Akademia Szerves Kemiai Technologiai Tanszek Selective hydrogenating catalysts and a process for the preparation thereof
US3943053A (en) * 1974-10-04 1976-03-09 Ashland Oil, Inc. Selective hydrogenation of aromatics and olefins in hydrocarbon fractions
US4049576A (en) * 1974-10-04 1977-09-20 Ashland Oil, Inc. Platinum-palladium catalyst for selective hydrogenation of aromatics and olefins in hydrocarbon fractions
US4018668A (en) * 1975-01-16 1977-04-19 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic sulfur-free catalytic composite
US3950243A (en) * 1975-03-14 1976-04-13 Universal Oil Products Company Hydrocarbon conversion with an acidic sulfur-free multimetallic catalytic composite
US3959121A (en) * 1975-05-05 1976-05-25 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic catalytic composite
US4097368A (en) * 1975-05-12 1978-06-27 Uop Inc. Hydrocarbon conversion with an acidic multimetallic catalytic composite
US3998724A (en) * 1975-05-12 1976-12-21 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic catalytic composite
US3972806A (en) * 1975-07-03 1976-08-03 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic catalyst composite
US4036903A (en) * 1975-08-08 1977-07-19 Uop Inc. Dehydrocyclization with an acidic multimetallic catalytic composite
US4079097A (en) * 1975-08-08 1978-03-14 Uop Inc. Normal paraffin hydrocarbon dehydrogenation with a nonacidic multimetallic catalytic composite
US3981795A (en) * 1975-08-08 1976-09-21 Uop Inc. Hydrocarbon conversion with an acidic multimetallic catalytic composite
US4139570A (en) * 1976-08-27 1979-02-13 Uop Inc. Dehydrogenation of naphthene hydrocarbons
US4384986A (en) * 1976-10-29 1983-05-24 Solvay & Cie. Particles of an alloy of noble metals with non-noble metals
US4179406A (en) * 1976-11-22 1979-12-18 Uop Inc. Acidic multimetallic catalytic composite
US4115252A (en) * 1976-11-22 1978-09-19 Uop Inc. Hydrocarbon conversion with an acidic multimetallic catalytic composite
US4233185A (en) * 1976-12-08 1980-11-11 Johnson, Matthey & Co., Limited Catalysts for oxidation and reduction
US4206042A (en) * 1978-03-31 1980-06-03 Uop Inc. Hydrocarbon dehydrocyclization with an acidic multimetallic catalytic composite
US4295957A (en) * 1979-04-30 1981-10-20 Exxon Research & Engineering Co. Reforming with multimetallic catalysts
US5409877A (en) * 1991-08-22 1995-04-25 Director-General Of Agency Of Industrial Science And Technology Catalyst for producing aldehyde and alcohol from olefin, carbon monoxide and hydrogen
US6548447B1 (en) * 1996-01-22 2003-04-15 Regents Of The University Of Minnesota Catalytic oxidative dehydrogenation process and catalyst
US6846773B1 (en) 1996-01-22 2005-01-25 Regents Of The University Of Minnesota Catalytic oxidative dehydrogenation process and catalyst
WO1998002242A1 (en) * 1996-07-15 1998-01-22 Chevron U.S.A. Inc. Sulfur resistant hydroconversion catalyst and hydroprocessing of sulfur-containing lube feedstock
US6030921A (en) * 1996-07-15 2000-02-29 Chevron U.S.A. Inc. Sulfur resistant hydroconversion catalyst and hydroprocess of sulfur-containing lube feedstock
US6136181A (en) * 1996-07-15 2000-10-24 Chevron U.S.A. Inc. Hydroconversion sulfur-containing lube feedstock using a sulfur resistant catalyst
US6264826B1 (en) 1996-07-16 2001-07-24 Chevron U.S.A Inc. Base stock lube oil manufacturing process
US5993644A (en) * 1996-07-16 1999-11-30 Chevron U.S.A. Inc. Base stock lube oil manufacturing process
US6462244B1 (en) * 1999-07-28 2002-10-08 Sũd-Chemie Inc. Hydrogenation catalysts
US20070181220A1 (en) * 2003-05-20 2007-08-09 Newman David M Method for making a nano-particulate medium
WO2004105007A1 (en) * 2003-05-20 2004-12-02 Coventry University Method for making a nano-particulate medium
US7811965B2 (en) * 2004-08-18 2010-10-12 Symyx Solutions, Inc. Platinum-copper-nickel fuel cell catalyst
US20060058185A1 (en) * 2004-08-18 2006-03-16 Symyx Technologies, Inc. Platinum-copper-nickel fuel cell catalyst
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NL7104741A (OSRAM) 1971-10-15
GB1332361A (en) 1973-10-03
CA938278A (en) 1973-12-11
BE765668A (fr) 1971-10-13
DE2117651A1 (de) 1971-10-28

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