Hydrocarbon reforming process using a zirconium oxide supported catalyst doped with tantalum

Abstract: Supports for catalytic reforming catalysts are prepared by doping ZrO₂ with tantalum. The catalyst may contain a Group VII or Group VIII metal and/or an acidic component.

Description: Background of Invention Catalytic reforming, or hydroforming, is a well established refinery process for improving the octane quality of naphthas or straight run gasolines. Reforming can be defined as the total effect of the molecular changes, or hydrocarbon reactions, produced by dehydrogenation of cyclohexanes, and dehydroisomerization of alkylcyclopentanes to yield aromatics; dehydrogenation of paraffins to yield olefins; dehydrocyclization of paraffins and olefins to yield aromatics; isomerization of n-paraffins; isomerization of alkylcycloaparaffins to yield cyclohexanes; isomerization of substituted aromatics; and hydrocracking of paraffins which produces gas, and inevitably coke, the latter being deposited on the catalyst. In catalytic reforming, a multifunctional catalyst is usually employed which contains a metal hydrogenation-dehydrogenation (hydrogen transfer) component deposited on a porous, inorganic oxide acidic support. An example of such a catalyst is detailed in FR2115860 which teaches the use of platinum together with either nickel or tantalum on a refractory support. All of the reforming catalysts in general use today contain platinum supported on an alumina or an alumina-silicate base. In many cases, rhenium is combined with platinum to form a more stable catalyst which permits operation at lower pressures. The platinum is thought to serve as a catalytic site for hydrogenation and dehydrogenation reactions and halogenated alumina provides an acid site for isomerization, cyclization, and hydrocracking reactions. Halide, particularly chloride, is known to be a catalyst promoter when added to a reforming catalyst. Zirconium oxide is also known as a support for platinum reforming catalysts but it has not achieved commercial success. Summary of Invention The present invention provides a process for catalytically reforming a hydrocarbon feedstock boiling in the gasoline-range with a zirconium oxide supported catalyst containing a metal selected from Group VII or Group VIII, characterised in that the zirconium oxide is doped with 0.1-20.0 weight percent tantalum. Detailed Description of Invention Our invention is a zirconium oxide based reforming catalyst containing a metal selected from Group VII or Group VIII and the use thereof in reforming. Zirconium oxide (ZrO 2 ) is an article of commerce and readily available. It exists as a lattice of zirconium atoms and oxygen atoms and the term "doping" in the art refers to the replacing of zirconium ion in the lattice with an ion of another metal, which in the present cases, is tantalum. Thus, doping is to be distinguished from, say, merely laying down tantalum or compounds of tantalum on the surface of zirconium oxide particles. Our zirconium oxide support is doped with 0.1-20% tantalum, preferably 0.5-10%, more preferably 1-5%. The doped zirconium is readily prepared by mixing appropriate amounts of compounds of the two metals followed by drying and calcining. This is shown in the examples which follow. Our catalysts also contain a Group VII or VIII metal, such as platinum, iridium, rhenium, nickel, ruthenium, iron, manganese, etc., preferably platinum. Many of these are known, alone or in combination, as reforming catalyst components. The amount of the Group VII or VIII metal will be .05-20%, usually .1-10%. In order to achieve the full benefits of the catalyst for reforming, an acidic component such as chlorided alumina can be combined with the doped zirconium oxide, usually in a ratio of the former to the latter of .1:1 to .9:1. The amount of chloride on the alumina is usually .01-2%. Other methods of imparting acidity to the zirconium oxide can also be used. See for example the sulfating procedures described in U. S. 4,956,519 and 4,918,041, which may be applied to the catalyst used in the process of the invention by sulfating cohydrolyzed zirconium and tantalum prior to calcining. Reforming operations with our catalysts can be carried out in known manner. Suitable feedstocks for reforming in accordance with the instant invention are any hydrocarbonaceous feedstock boiling in the gasoline range. Examples of such feedstocks include the light hydrocarbon oils boiling from about 21° to about 260°C (70° to about 500°F.), preferably from about 82° to about 204°C (180° to about 400°F). Examples of such feedstocks include straight run naphtha, synthetically produced naphtha, thermally or catalytically cracked naphtha, hydrocracked naphtha, or blends or fractions thereof. Reforming is usually carried out at 500-1500°C at a hydrogen to hydrocarbon ratio of 1:1-10:1, usually 2:1-5:1. Pressures of 689-6895 kPa (100-1000 psig) and a LHSV of 1-3 are customary for semi-regenerative units. Lower pressures are customary for continuously regenerating units. Examples The doped zirconias were prepared by cohydrolysis of zirconium n-propoxide and tantalum ethoxide by mixing solutions of these in isopropanol to appropriate proportions of Zr:Ta. These alkoxides were purchased. The combined solutions were added dropwise with stirring to a solution of a slight excess of NH 4 OH in water/isopropanol solvent. Temperature was maintained at about 30°C by a cold water jacket for one hour while stirring. The precipitate was then filtered and dried overnight at 110°C followed by calcination in a static bed in air at 900°C for five hours. To prepare the catalyst, a 250 ml beaker was charged with the appropriate quantity of a solution of chloroplatinic acid which was then diluted with water. While this solution was being stirred, the required amount of support was added and stirring continued for about one half hour to allow the solution to soak into the catalyst carrier. This was followed by gentle heating until most of the water was evaporated and stirring became difficult. Heating was reduced and maintained until the water had almost completely evaporated. The resulting solid residue was dried in an oven at about 100°C to remove any remaining water. To reduce the metal compounds, the catalyst was heated at 200°C for one hour in nitrogen flow. After the last traces of water were driven off, the solid was reduced in hydrogen flow at the same temperature for five hours. Subsequent to reduction, the catalyst was cooled in nitrogen flow and then stored until use. Normally, catalysts used were 20 mesh size pellets. However, when alumina was added as a physical mixture, the initial mixing of the catalyst with alumina was done using powders in a mortar and pestle. The physically mixed samples were then pelletized. The pellets were then broken and sieved to the correct size of 20 mesh. Reforming studies were carried out with n-heptane at temperatures of about 500°C and a hydrogen/heptane ratio of 6:1. The pressure was about 1034 kPa (150 psig). Results are shown in the Tables below. The rates shown in the Tables are x10 -3 and are per mol of heptane converted per gram of catalyst (exclusive of any added alumina) per hour. Table 1 shows the effect of 0.5% platinum on ZrO 2 without the further addition of an acidic component. It is evident that the addition of tantalum to the zirconium doubles the dehydrocyclization activity of the zirconium catalyst and increases isomerization as well. Dehydrocyclization refers to the formation of benzene and toluene and isomerization to the formation of isoheptane. EFFECT OF DOPING Pt/ZrO 2 WITH Ta 2 0 5 Rate Weight % Ta 2 O 5 0.0 1.0 2.0 Temperature °C 495 501 494 Dehydrocyclization 1.07 2.72 2.44 Isomerization 0.00 0.39 1.83 Cracking 0.00 0.00 0.00 C 5 -C 6 0.00 0.00 0.00 Toluene 0.00 0.50 0.64 Table 2 shows the use of 0.5% Pt on 2% Ta 2 O 5 and on undoped ZrO 2 blended 1:1 with chlorided gamma alumina in comparison with a commercial Pt + Re reforming catalyst, PR-8. Excellent selectivity is observed for dehydrocyclization plus isomerization with little molecular weight reduction or cracking. This translates to a liquid reformate yield increase over Pt/2% Ta 2 O 5 -ZrO 2 + Cl/Al 2 O 3 compared to PR-8. EFFECT OF ADDITION OF 1% CHLORIDED ALUMINA Catalyst PR-8 Pt/ZrO 2 /1% Chlorided Alumina Pt/ZrO 2 /2% Ta 2 O 5 /1% Chlorided Alumina Temp.° 498 500 497 500 Rate Dehydrocyclization 13.24 7.22 9.23 9.16 Isomerization 38.16 15.91 38.28 27.74 Cracking 5.49 2.82 2.21 3.97 C 5 -C 6 9.30 4.92 5.42 5.13 Toluene 5.10 1.77 4.31 5.27

Claims: A process for catalytically reforming a hydrocarbon feedstock boiling in the gasoline-range with a zirconium oxide supported catalyst containing a metal selected from Group VII or Group VIII, characterised in that the zirconium oxide is doped with 0.1-20.0 weight percent tantalum. A process according to Claim 1, wherein the zirconium oxide is doped with 0.5-10.0 weight percent tantalum. A process according to Claim 1 or 2, wherein said Group VII or VIII metal is platinum or nickel. A process according to any of Claims 1 to 3, wherein said catalyst also contains an acidic component. A process according to Claim 4, wherein said acidic component is chlorided alumina. A process according to any of Claims 1 to 5, wherein said zirconium is sulfated to provide acidity.

Inventors: DURANTE VINCENT A, MACRIS ARISTIDES, PITCHAI RANGASAMY, VERYKIOS XENOPHON E, DURANTE, VINCENT A., MACRIS, ARISTIDES, PITCHAI, RANGASAMY, VERYKIOS, XENOPHON E.
Applicants: SUN CO INC R & M, SUN COMPANY, INC. (R&M)
Application year: 1992
Main classification: C10G35
IPC codes: B01J27, C10G45, B01J23, B01J32, C07C61, C10G35