US3827988A - Pt-pb catalyst compositions - Google Patents

Pt-pb catalyst compositions Download PDF

Info

Publication number
US3827988A
US3827988A US00200065A US20006571A US3827988A US 3827988 A US3827988 A US 3827988A US 00200065 A US00200065 A US 00200065A US 20006571 A US20006571 A US 20006571A US 3827988 A US3827988 A US 3827988A
Authority
US
United States
Prior art keywords
catalyst
lead
platinum
percent
carrier
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US00200065A
Other languages
English (en)
Inventor
N Kominami
T Iwaisako
K Ohki
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Asahi Kasei Corp
Asahi Chemical Industry Co Ltd
Original Assignee
Asahi Chemical Industry Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Asahi Chemical Industry Co Ltd filed Critical Asahi Chemical Industry Co Ltd
Application granted granted Critical
Publication of US3827988A publication Critical patent/US3827988A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • This invention relates to a Pt-Pb catalyst compositions which can also contain one or more other catalytic components, and to methods for their preparation. It is also concerned with a method of producing a distillate of high aromatic concentration in high yield by highly selectively subjecting naphthenic hydrocarbons 0t dehydrogenation and paratfinic hydrocarbons to dehydrocyclization, by contacting such hydrocarbons with the catalysts.
  • the present invention derived from the discovery, is concerned with a method of producing aromatic hydrocarbons which comprises treating a hydrocarbon or a hydrocarbon mixture at a temperature from 300 C. to 650 C.
  • a catalyst comprising platinum and lead or a catalyst comprising platinum, lead and at least a member selected from lithium, sodium, potassium, rubidium, cesium, beryllium, magnesium, calcium, strontium, barium, zinc, cadmium, mercury, germanium, bismuth, chromium, molybdenum, tungsten, uranium, rhenium, ruthenium, rhodium, palladium, osmium and iridium.
  • the catalyst is prepared by an impregnation procedure.
  • benzene, toluene, xylenes and polymethylbenzenes are produced by quite simple procedures at low cost because of high concentration and yield of aromatics in the reformate produced according to this invention.
  • a distillate of higher boiling point than toluene or xylene in the reaction product contains neither paraffin nor naphthene and then separation can be effected by distillation only, without application of solvent extraction.
  • Such a distinction from the prior processes is ascribed to high activity and selectivity of the catalyst of this invention in terms of aromatic formation, namely dehydrogenation or dehydrocyclization reactions.
  • life of the catalyst of this invention is so long that frequency in regeneration of the catalyst is reduced under normal reaction conditions in industrial operation.
  • the catalyst of this invention is operative at lower pressures than in prior processes.
  • the rate of degradation in activity in the prior catalysts is much more drastic and they become inoperative during long operation, and, therefore, the process on an industrial scale has to be carried out under high pressures.
  • the catalyst of this invention is stable in the course of a long operation to give a high yield of aromatics.
  • platinum component of the catalyst there may be used, for example, the hydroxide, platinum halides, chloroplatinic acid or hydrate or ammonium salt thereof. Especially preferred are substances containing a halogen.
  • the halogen and especially chlorine present in the compound advantageously contribute to the catalytic activity like in other platinum reforming cata lysts.
  • the preferable amount of chlorine contained in the catalyst of the present invention is in the range of 0.1- 2.0% by weight and particularly in the range of. 0.5-1.5% by weight based on the total weight of catalyst compo. nents.
  • the lead component there may be employed halogenides, inorganic and organic salts, hydroxide, oxide and the like.
  • the element used as the third component may be in the form of its oxide, hydroxide, halide or other inorganic and organic salt or complex.
  • the platinum, lead and the third components may be in the form of a salt containing each of them.
  • Contents of the platinum, lead and the third components are 0.0l% by weight, 0.015% by weight and 03% by weight, respectively, and preferably 0.051% by weight, ODS-3% by weight and 04% by weight, respectively based on the total weight of catalyst components, with the ratio of lead to platinum ranging from 0.1 to 3.
  • the catalyst is prepared by simultaneously supporting platinum and lead on a carrier by conventional impregnation methods; or by supporting lead on a carrier and thereafter supporting platinum on the carrier, again using conventional impregnation methods.
  • Preferred Pb/Pt ratios, lead and platinum contents, and third component content with the two impregnation methods are as follows:
  • a carrier is immersed in a solution (normally an aqueous solution) containing platinum and lead components, thereby supporting both of said components simultaneously on the carrier.
  • a solution normally an aqueous solution
  • the amount of solution used is preferably from 1 to volumes per volume of the carrier for economical reasons.
  • solvent is removed either by vaporation into dryness or filtration.
  • the catalyst is then calcined at a temperature from 400 C. to 700 C., preferably 450 C. to 600 C.
  • the catalyst is prepared by immersing a carrier in an aqueous solution containing a lead compound such as, e.g., lead nitrate and lead chloride, to support the lead component on the carrier, drying the resulting material and then calcining the dried product at a temperature ranging from 300 C. to 800 C.
  • the calcined product is then immersed in an aqueous solution containing a platinum compound such as, e.g., chloroplatinic acid, to support the platinum component thereon, drying the resulting assembly and then calcining the dried product at a temperature ranging from 400 C. to 700 C., preferably from 450 C. to 600 C.
  • ⁇ amounts of platinum, lead and a third component contained in the solution of platinum compound, lead compound and third component are, in general, 0.01-5 wt. percent platinum; 0.01-5 wt. percent lead and 0-3 wt. percent third component.
  • the ranges preferably are 0.1l wt. percent platinum; 0.1-2 wt. percent lead and 0-1 wt. percent third component.
  • the ranges preferably are 0.1-1 wt. percent platinum; 0.1-25 wt. percent lead and 0-1 wt. percent third component.
  • Lead to platinum weight ratio in the solution generally ranges from 0.1 to 3.0, and preferably, in the simultaneous impregnation method, it ranges from 0.3 to 2.0, and in the sequential impregnation method, it ranges from 0.3 to 2.5.
  • the proportion of contents of the components depends, for example, upon the type of carrier, surface area, order of the addition, method of the calcination and the like.
  • a carrier such as silica alumina, alumina, alumina hydrate, silica, zeolite, kaolin, acid clay or bentonite is eifective and preferable carriers are alumina, silica alumina, zeolite and the like.
  • hydrocarbons which may be used in the present invention as the starting material include those mainly comprising parafiins, olefins and naphthenes having a boiling point point within the range of from 40 to 350 C., which may be used alone or in admixture of two or more kinds.
  • Preferable hydrocarbons are those having from 6 to 12 carbon atoms.
  • Feeding ratio of hydrogen to hydrocarbon in gas volume is from 0.5 to 15 and preferably from 2 to 10.
  • the catalyst Prior to the reaction, the catalyst may be pretreated with hydrogen at or near the reaction temperature to activate it.
  • Feeding rate of the hydrocarbon in terms of LHSV which stands for liquid hourly space velocity, (the feeding amount of hydrocarbon per unit time, per unit volume of catalyst, in ml.) is from 0.2 to 10 hr. and preferably from 0.5 to 5 hr.-
  • reaction pressure is dependent upon the desired quality of product and economy and may be optionally chosen whithin the range of from 1 to 50 kg./cm. and
  • reaction is preferably carried out under an elevated pres sure.
  • Example 1 In an aqueous solution of a mixture of chloroplatinic acid and lead chloride was immersed 'y-alumina. After being dried, the resulting mass was calcined at 550 C. for 2 hours to prepare a catalyst with a composition: 0.5%Pt-0.25%Pb-Al O Percent is by weight herein unless otherwise noted.
  • Example 2 A hundred milliliters of a catalyst prepared by the same method as in Example 1, the compositions being 0.5%Pt-0.5%Pb-Al O was heated under hydrogen at 500 C. for 2 hours. Through the catalyst layer was passed a gaseous mixture of hydrogen and naphtha with the composition given below at a feeding ratio of 3:1 (by gas volume) at an LHSV of 2.0 hr? under a total reaction presure of 10 kg./cm. (gauge) continuously for 48 hours, while maintaining the layer at a temperature of 500 C. Yields by weight of the products were: Hydrogen 4.5%, benzene 5.4%, toluene 15.3%, xylenes 30.6% and the total aromatics 76.7%.
  • Example 4 With 100 cc. of a catalyst composition comprising 0.5% platinum, 0.5 lead and 'y-alumina was supported 0.3% potassium carbonate by impregnation and after the catalyst was reduced by hydrogen for an hour at 530 C., a gaseous mixture of hydrogen and naphtha having a composition shown below in a volume ratio of 10:1 was passed therethrough at an LHSV of 1.0 hr.- at a reaction temperature of 480 C. under a reaction pressure of 4 l-:g./cm. (gauge).
  • Catalyst composition Pt-Pb-K COs Reaction time (hr.) 20 100 200 Composition of liquid (wt. percent):
  • Example 5 'y-Alumina granulated in a ball of a diameter of 2 mm. was immersed in an aqueous solution of rubidium hydroxide, followed by drying and calcination at 570 C. to give a carrier of the composition 0.21% rubidium-99.79% A1 0 The carrier was then immersed in an aqueous solution of a mixture of chloroplatinic acid and lead chloride. After being dried in 2 hours and calcined at 550 C. for 2 hours, there was prepared a catalyst of the composition: 0.5% Pt-0.5% Pb-0.2% Rb-Al O A reactor 1.25 inches in diameter Was filled with the catalyst and treated under hydrogen for 45 minutes during which period the temperature was raised from 410 C. to 530 C.
  • a gaseous mixture of hydrogen and naphtha with the composition given below in a ratio of 7.5 :1 was passed through the reaction tube at an LHSV of 2.0 hr. and a temperature of 510 C. under a pressure of 10 kg./cm. Yields by weight on average of the products after 25 hrs., on the naphtha basis, were: Benzene 4.4%, toluene 14.9%, xylenes 33.6% and the total aromatics 77.9%.
  • Example 6 'y-Alumina was immersed in an aqueous solution of a mixture of bismuth nitrate, lead nitrate and chloroplatinic acid, followed by drying and calcination at 530 C. for 4 hours to prepare a catalyst of the composition of 0.4% Pt-0.5% Pb-0.6% Bi-Al O Reaction was conducted using ml. of the catalyst under a pressure of 14 kg./cm. at an LHSV of 2.4 hr? for 20 hrs. by the same method as in Example 1. The yields by weight were: Benzene 2.9%, toluene 13.3%, xylenes 29.3% and the total aromatics 71.5%. 1
  • Example 28 In 200 cc. of an aqueous solution containing 0.0128 mol./ liter of chloroplatinic acid and 00036-00605 mol./
  • compositions of the resulting catalysts are 0.5 wt. percent Pt; 0.15-2.50 wt. percent Pb and A1 while Pb/ Pt ratio is from 0.3 to 5.0.
  • a mixed gas consisting of hydrogen and n-heptane in a molar ratio of 3:1 was passed through the catalyst layer maintained at 490 C. under atmospheric pressure at a liquid hourly space velocity of 0.5 hrr.
  • Example 29 After 20 cc. of the resulting catalyst were heated at In 200 cc. of an aqueous solution containing 0.0072 0.122 mol./ liter of lead nitrate were immersed 140 cc. of 'y-alumina having a particle size of 23 mm. diameter as a carrier, then, after vaporized to dryness, calcined at 550 C. for 3 hours, and, subsequently, immersed in 200 cc. of an aqueous solution containing 0007-2026 moL/iiter of chloroplatinic acid, followed by vaporizing to dryness and calcining at 550 C. for 3 hours.
  • the resulting catalyst had a composition of 0.3-1.0 wt. percent Pt; 0.3-5.0 wt. percent Pb and A1 0 while Pb/ Pt ratio was within the range of 0.5-5.0.
  • Comparative Example 1 20 cc. of a known catalyst comprising 0.5% Pt and 99.5% 'y-alumina were heated at 500 C. under a hydrogen stream for an hour. Then, there was passed a mixed gas consisting of hydrogen and n-heptane in a molar ratio of 3:1 through the catalyst layer maintained at 500 C. under atmospheric pressure at a liquid hourly space velocity of 0.5 hr. As a result, molar yields of the resulting products were as follows:
  • Comparative Example 2 Twenty milliliters of a known catalyst consisting of 0.5% platinum and 99.5% 'y-alumina were heated under hydrogen at 500 C. for 1 hour. Through the catalyst layer was passed a gaseous mixture of hydrogen and n-heptane at an LHSV of 0.5 hr.- under atmospheric pressure, while maintaining the layer at 510 C. Molar yields of the products were: Benzene 8.7%, toluene 36.7%, xylenes 3.8% and the total aromatics 49.2% after a reaction time of 1 hour.
  • the catalysts described herein can also be used for conversion of hydrocarbons such as hydrocracking, isomerization and dehydrogenation.
  • a catalyst composition comprising from about 0.01 to about 5 weight percent of platinum, from about 0.01 to about 5 weight percent of lead, up to 2.0 weight percent of a halogen, and the balance a carrier, wherein the ratio of lead to platinum is from 0.3 to 2.5, said catalyst being prepared by simultaneously supporting said platinum and lead components on said carrier by impregnation, or first supporting said lead component on said carrier by impregnation and thereafter supporting said platinum component on said carrier by impregnation.
  • a catalyst composition according to Claim 1 wherein a third component selected from the group consisting of lithium, sodium, potassium, rubidium, cesium, berylium, magnesium, calcium, strontium, barium, Zinc, cadmium, mercury, germanium, bismuth, chromium, molybdenum, tungsten, uranium, rhenium, ruthenium, rhodium, palladium, osmium and iridium, is supported on the carrier in an amount of up to about 3 weight percent.
  • a third component selected from the group consisting of lithium, sodium, potassium, rubidium, cesium, berylium, magnesium, calcium, strontium, barium, Zinc, cadmium, mercury, germanium, bismuth, chromium, molybdenum, tungsten, uranium, rhenium, ruthenium, rhodium, palladium, osmium and iridium, is supported on the carrier in an amount of up to about
  • a catalyst composition according to Claim 2 wherein said third component is incorporated before, after or simultaneously at the time of supporting both said platinum and lead components on said carrier.
  • a catalyst composition according to Claim 2 wherein said catalyst contains from about 0.1 to about 1 wt. percent platinum, from about 0.1 to about 2 wt. percent lead and from 0 to about 1 wt. percent third component, wherein the ratio of lead to platinum ranges from 0.3 to 2.0, and is prepared by a simultaneous impregnation method.
  • a catalyst composition according to Claim 2 wherein said catalyst contains from about 0.1 to about 1 wt. percent platinum, from about 0.1 to about 2.5 wt. percent lead and from 0 to about 1 wt. percent third component, and is prepared by said sequential impregnation method.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US00200065A 1969-02-10 1971-11-18 Pt-pb catalyst compositions Expired - Lifetime US3827988A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP948869 1969-02-10
JP6761769 1969-08-28
JP10381769 1969-12-25

Publications (1)

Publication Number Publication Date
US3827988A true US3827988A (en) 1974-08-06

Family

ID=27278502

Family Applications (3)

Application Number Title Priority Date Filing Date
US00200071A Expired - Lifetime US3827973A (en) 1969-02-10 1971-11-18 Reforming with a coprecipitated platinum-lead catalyst
US00200065A Expired - Lifetime US3827988A (en) 1969-02-10 1971-11-18 Pt-pb catalyst compositions
US00200064A Expired - Lifetime US3827972A (en) 1969-02-10 1971-11-18 Method of producing aromatic hydrocarbons

Family Applications Before (1)

Application Number Title Priority Date Filing Date
US00200071A Expired - Lifetime US3827973A (en) 1969-02-10 1971-11-18 Reforming with a coprecipitated platinum-lead catalyst

Family Applications After (1)

Application Number Title Priority Date Filing Date
US00200064A Expired - Lifetime US3827972A (en) 1969-02-10 1971-11-18 Method of producing aromatic hydrocarbons

Country Status (4)

Country Link
US (3) US3827973A (enrdf_load_stackoverflow)
DE (1) DE2005828C3 (enrdf_load_stackoverflow)
GB (1) GB1305137A (enrdf_load_stackoverflow)
NL (1) NL162353C (enrdf_load_stackoverflow)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3915846A (en) * 1973-04-23 1975-10-28 Universal Oil Prod Co Hydrocarbon conversion with a trimetallic catalytic composite
US3928177A (en) * 1972-01-10 1975-12-23 Universal Oil Prod Co Hydrocarbon conversion with a multimetallic catalytic composite
US3980726A (en) * 1973-06-01 1976-09-14 Universal Oil Products Company Dehydrogenation with a nonacidic multimetallic catalyst
US4028225A (en) * 1974-06-13 1977-06-07 Uop Inc. Hydrocarbon conversion with a sulfided acidic multimetallic catalytic composite
US4053389A (en) * 1974-06-13 1977-10-11 Uop Inc. Hydrocarbon conversion with an acidic multi-metallic catalytic composite
US4072602A (en) * 1972-01-10 1978-02-07 Uop Inc. Dehydrogenation method and nonacidic multimetallic catalytic composite for use therein
US4130597A (en) * 1975-07-21 1978-12-19 Wilhelm Frederick C Dehydrogenation using multimetallic catalyst
US4939110A (en) * 1988-10-17 1990-07-03 Uop Catalyst for the isomerization of aromatics

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1390182A (en) * 1971-03-16 1975-04-09 Johnson Matthey Co Ltd Catalysis
JPS51963B1 (enrdf_load_stackoverflow) * 1971-07-05 1976-01-13
US3900387A (en) * 1972-03-10 1975-08-19 Universal Oil Prod Co Hydrocarbon conversion with a multimetallic catalytic composite
US3940329A (en) * 1974-01-24 1976-02-24 Universal Oil Products Company Hydrocarbon conversion with a multimetallic catalytic composite
DE3306907A1 (de) * 1983-02-26 1984-08-30 Basf Ag, 6700 Ludwigshafen Katalysator und seine verwendung zur herstellung von methylmethacrylat
FR2666249B1 (fr) * 1990-09-03 1994-07-22 Inst Francais Du Petrole Catalyseur et procede d'aromatisation des hydrocarbures contenant 2 a 4 atomes de carbone par molecule.
US5268522A (en) * 1990-09-03 1993-12-07 Institut Francais De Petrole Process for the aromatization of hydrocarbons containing 5 to 9 carbon atoms per molecule in the presence of a particular catalyst
FR2674769B1 (fr) * 1991-04-04 1994-04-29 Inst Francais Du Petrole Catalyseur du type galloaluminosilicate contenant du gallium, un metal noble de la famille du platine et au moins un metal additionnel, et son utilisation en aromatisation des hydrocarbures.
FR2840548B1 (fr) * 2002-06-07 2005-03-18 Inst Francais Du Petrole Lit homogene de catalyseur et procede de transformation d'hydrocarbures en composes aromatiques avec ledit lit
US9242233B2 (en) 2012-05-02 2016-01-26 Saudi Basic Industries Corporation Catalyst for light naphtha aromatization
US9180441B2 (en) 2012-09-20 2015-11-10 Saudi Basic Industries Corporation Method of forming zeolite shaped body with silica binder
US9782758B2 (en) 2013-04-23 2017-10-10 Saudi Basic Industries Corporation Method of preparing hydrocarbon aromatization catalyst, the catalyst, and the use of the catalyst
CN112742382B (zh) * 2019-10-29 2024-01-05 中国石油化工股份有限公司 一种催化重整催化剂的制备方法

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3928177A (en) * 1972-01-10 1975-12-23 Universal Oil Prod Co Hydrocarbon conversion with a multimetallic catalytic composite
US4072602A (en) * 1972-01-10 1978-02-07 Uop Inc. Dehydrogenation method and nonacidic multimetallic catalytic composite for use therein
US3915846A (en) * 1973-04-23 1975-10-28 Universal Oil Prod Co Hydrocarbon conversion with a trimetallic catalytic composite
US3980726A (en) * 1973-06-01 1976-09-14 Universal Oil Products Company Dehydrogenation with a nonacidic multimetallic catalyst
US4028225A (en) * 1974-06-13 1977-06-07 Uop Inc. Hydrocarbon conversion with a sulfided acidic multimetallic catalytic composite
US4053389A (en) * 1974-06-13 1977-10-11 Uop Inc. Hydrocarbon conversion with an acidic multi-metallic catalytic composite
US4130597A (en) * 1975-07-21 1978-12-19 Wilhelm Frederick C Dehydrogenation using multimetallic catalyst
US4939110A (en) * 1988-10-17 1990-07-03 Uop Catalyst for the isomerization of aromatics
AU625781B2 (en) * 1988-10-17 1992-07-16 Uop Isomerization catalyst and method for the use thereof

Also Published As

Publication number Publication date
NL162353B (nl) 1979-12-17
NL7001852A (enrdf_load_stackoverflow) 1970-08-12
US3827972A (en) 1974-08-06
GB1305137A (enrdf_load_stackoverflow) 1973-01-31
DE2005828B2 (de) 1973-08-09
US3827973A (en) 1974-08-06
DE2005828A1 (de) 1970-09-03
NL162353C (nl) 1980-05-16
DE2005828C3 (de) 1974-03-07

Similar Documents

Publication Publication Date Title
US3827988A (en) Pt-pb catalyst compositions
US3915845A (en) Hydrocarbon conversion with a multimetallic catalytic composite
US4157989A (en) Superactive multimetallic catalytic composite
US3511888A (en) Paraffin conversion catalyst and process
US4363721A (en) Method of using catalysts for reforming or isomerizing hydrocarbons in the presence of hydrogen
RU2547466C1 (ru) Катализатор и способ реформинга
US5128300A (en) Reforming catalyst with homogeneous metals dispersion
US3770616A (en) Method of reforming hydrocarbons
US4548918A (en) Process for manufacturing a hydrocarbon conversion catalyst and catalyst prepared by said process
US4964975A (en) Reforming catalyst with homogeneous metals dispersion
US3801498A (en) Tetrametallic hydrocarbon conversion catalyst and uses thereof
US3578584A (en) Hydrocarbon conversion process and platinum-germanium catalytic composite for use therein
US3898154A (en) Hydrocarbon conversion with a multimetallic catalytic composite
US2848510A (en) Manganese reforming oxide-containing catalyst
US3796654A (en) Hydrocarbon conversion with a multicomponent catalyst
US3806446A (en) Reforming of hydrocarbons with a platinum-tungsten-germanium catalyst
US3928177A (en) Hydrocarbon conversion with a multimetallic catalytic composite
EP0018808B1 (en) Pd/pt catalyst composition for hydrocarbon reforming and reforming process using same
US4246095A (en) Hydrocarbon conversion with a sulfided superactive multimetallic catalytic composite
US3875048A (en) Reforming process using platinum-lead-third component catalyst and catalyst therefor
US4048099A (en) Hydrocarbon conversion with an acidic trimetallic catalytic composite
US3827971A (en) Reforming with platinum-lead catalyst
US4072731A (en) Dehydrocyclization with an acidic multimetallic catalytic composite
US4238366A (en) Attenuated superactive multimetallic catalytic composite
US4261811A (en) Reforming with an improved rhenium-containing catalyst