Isomerisation catalysts for hydrocarbons - contg platinum group metal, halogen and metal halide and rhenium or germanium cpds

The catalysts consists of (A) an alumina carrier, (B) a Pt gp. metal (C) a halogen, (D) a Friedel-Crafts metal halide and (E) a Re or Ge component, the Ge being in an oxidn. stage higher than elementary Ge. Content of Re is pref. 0.01-1 wt % or of Ge pref 0.01-5 wt %, pref. in the form of GeO2. Amount of (B) is pref 0.01-1% and of (C) 0.1-5% (D) is pref. present in amt. of 1-100 wt% of the remaining catalyst. The catalyst may be pre-sulphided to a S content of 0.05-0.5 wt %. They are suitable for isomerisation of olefines, paraffins, cycloparaffins and/or alkyl aromatics, in presence of H2 e.g. in prodn of p-xylene or high octane petrols.

HYDROCARBON CONVERSION

SELECTIVELY SOUR ONE CATALYST COMPOSITION SULFIDIERTE.

VERFAHREN ZUR UMWANDLUNG VON KOHLENWASSERSTOFFEN UND KATALYSATOR ZU SEINER DURCHFUEHRUNG

Improved Catalytic Reforming.

... 1,182,972. Reforming. UNIVERSAL OIL PRODUCTS CO. 26 June, 1967 [27 June, 1966], No. 29332/67. Heading C5E. In a catalytic reforming process wherein a hydrocarbon charge is contacted at elevated temperature and pressure and in a reforming zone with a gas containing hydrogen and with a catalytic composite comprising a platinum group metallic component and a refractory inorganic oxide component, the contact is effected in an essentially water-free environment and in the presence of from 10 to 3000 ppm. of sulphur by weight of the charge stock. The metallic component may be Pt, Pd, Rh, Ru, Os or Ir; it may exist as halide or sulphide. The refractory oxide may be alumina, silica, boria, zirconia, magnesia, thoria, titania or strontia or mixtures, e.g. silica-alumina, alumina-boria or silica-alumina-zirconia. Suitable feeds include gasoline and naphtha. The sulphur may be added as a compound reducible to H 2 5.

PROCESS FOR REGENERATING COKE-DEACTIVATED CATALYST

... 1293632 Reforming naphtha UNIVERSAL OIL PRODUCTS CO 9 March 1970 [7 March 1969] 11113/70 Heading C5E [Also in Division B1] A heavy naphtha is reformed under a pressure of 100 p.s.i.g., at 973-1022, LHSV 1À5 hr.-1 and a hydrogen : hydrocarbon molar ratio of 9 : 1, the temperature being continuously adjusted to give an octane of 102 F-1 clear for the C 5+ reformate, over a Pt, Re, Cl on Al 2 O 3 catalyst which has been regenerated by treatment (a) with 1% O 2 , 1% H 2 O, 0À014% HCl and N 2 at 475‹ C., (b) the same gas mixture at 510‹ C., (c) 21% O 2 , 3% H 2 O, 0À042% HCl and N 2 at 510‹ C., (d) 17À0% O 2 , 18À5% H 2 O, 0À3% HCl and N 3 at 525‹ C., and finally (e) dry H 2 at 566‹ C. after purging with N 3 . All the regenerant gases were at 5 p.s.i.g.

CATALYST AND HYDROCARBON CONVERSION

CATALYST AND HYDROCARBON CONVERSION

ACIDIC MULTIMETALLIC CATALYTIC

ISOMERIZATION OF HYDROCARBONS

Improved Liquefied Petroleum Gas Reforming Process

... 1,184,196. Reforming. UNIVERSAL OIL PRODUCTS CO. 12 July, 1967 [13 July, 1966], No. 32087/67. Heading C5E. A process for the production of a high octane reformate and a high yield of normally gaseous hydrocarbons having three and four carbon atoms from a hydrocarbon charge stock wherein said charge stock and hydrogen are contacted in a reforming zone with a catalytic composite containing a finely divided crystalline aluminosilicate suspended in an alumina matrix, and having at least one active catalytic component composited therewith comprises pressurizing said reforming zone with hydrogen to a level within a range of from 5.1 to 10-2 atmospheres gauge, circulating hydrogen through said reforming zone while heating the latter to a temperature within a range of from 775‹ to 825‹ F., introducing said hydrocarbon charge stock to said zone, raising the temperature of said reforming zone at an average rate of from 5‹ to 30‹ F. per hour to a temperature within the range of from 925‹ to 1000‹ ...

Improved Catalytic Reforming for Liquefied Gas Production.

1,182,818. Reforming; gaseous hydrocarbons. UNIVERSAL OIL PRODUCTS CO. 26 June, 1967 [27 June, 1966], No. 29331/67. Heading C5E. In a process for the production of high octane reforrnate and a high yield of normally gaseous hydrocarbons having three or four carbon atoms from a hydrocarbon charge stock, the charge stock and hydrogen are contacted in a reforming zone with a catalytic composite containing a finely divided crystalline alumino - silicate suspended in an alumina matrix, and having at least one active catalytic component composited therewith, the contact being effected in the presence of from 10 to 5000 p.p.m. sulphur by weight of the charge stock. The catalytic component may be platinum or nickel and/or chlorine or fluorine. The preferred aluminosilicate is a hydrogen mordenite. The catalyst may be sulphided. Suitable charge stocks are gasoline or naphtha fractions.

MANUFACTURE OF METAL OXIDE SOLS

... 1,212,041. Continuous sol production. UNIVERSAL OIL PRODUCTS CO. 18 June, 1968 [21 June, 1967], No. 29009/68. Heading C1A. A metal oxide sol is produced continuously by reacting, in a digestion zone, an excess of particles of aluminium, chromium, iron, zirconium; zinc, gallium, or mixtures thereof, with a mixture of hydrochloric acid and recycled sol by passing the mixture through the digestion zone at a superficial linear velocity (defined as volume flow rate over area of digestion zone when empty) of at least 31 cm/minute and continuously removing part of the resultant sol at a rate such that the average residence time of the sol in the digestion zone is from 1 to 12 hours, the remainder of the sol being recycled. The linear velocity of the acid/sol mixture in the digestion zone may be as high as 610 cm/minute. The temperature in the digestion zone may be 52‹ C. to 121‹ C., and pressure may be applied to maintain the sol/acid mixture in the liquid phase e.g. by controlled venting of the ...

VERFAHREN ZUR DEHYDRIERUNG VON KOHLENWASSERSTOFFEN UND KATALYSATOR ZU SEINER DURCHFUEHRUNG

REGENERATION OF DEACTIVATED CATALYST CONTAINING A PLATINUM GROUP COMPONENT AND A SULFUR COMPONENT

... 1278119 Catalyst regeneration UNIVERSAL OIL PRODUCTS CO 2 Dec 1969 58707/69 Heading B1E [Also in Division C5] A catalyst containing a platinum group component and a sulphur component and which has been used in a hydrocarbon conversion process is regenerated by: (a) stopping contact of the hydrocarbon charge stock with the catalyst; (b) reducing the sulfur content of the catalyst to less than 0.02 wt. % by contacting the catalyst, without intervening treatment, with a sulphur-free and water free hydrogen stream, suitably at 430 to 595‹C and a pressure of 3.4 to 24 atmospheres gauge; (c) removing the substantial portion of the carbonaceous deposit by treating with oxygen, suitably at 370 to 595‹C; (d) purging free oxygen from the treated catalyst; (e) reducing the platinum group component by contact with a sulphurfree and water-free hydrogen stream, suitably at 480 to 595‹C; and (f) incorporating 0.05 to 0.50 wt. % of sulphur in the catalyst by treatment with an oxygen free sulphiding gas ...

USE OF GUARD BEDS IN HYDROCARBON CONVERSION WITH A

CATALYTIC COMPOSITE

Trimetallic, acidic, dual-function catalyst

The catalyst comprises 0.01-2 wt.% Pt or Pd (pref. 0.05-1 wt.% Pt) and 0.01-2 (&ref. 0.05-1) wt.% Ir, 0.01-5 (pref. 0.05-2) wt.% Ge and 0.1-3.5 (pref. 0.5-1) wt.% halogen, esp. Cl, the metals being uniformly dispersed throughout a porous refractory inorg. oxide, and esp. alumina, carrier, the Ge being present as an oxide. The process is carried out at 800-1100 (pref. 900-1050) degrees F, up to 100 psig (pref. 50-350 psig), an LHSV of 0.1-10 (pref. 1-5) and an H2/hydrocarbon molar ratio of 1-20 : 1 (pref. 5-10). The catalyst has improved characteristics, including relative insensitivity to hydrocarbon deposn., a lower C5 + yield loss for a given temp.increase and increased hydrogen prodn ...

Hydrocarbon conversion, esp. gasoline reforming - with catalyst contg. cobalt, tin, platinum gp. metal and halogen, which has high activity and is resistant to deactivation

Hydrocarbons are converted on an acidic catalyst consisting of (a) a porous carrier contg. (b) 0.01-2 wt.% Pt. gp. metal (0.05-1%), (c) 0.1-5 (0.5-2)% Co, (d) 0.01-5 (0.05-2)% Sn, and (e) 0.1-3.5 (0.5-1.5)% halogen. The Pt. gp. metal, catalytically available Co, and Sn are uniformly distributed through the carrier. The average crystallite size of the Co and Sn is 100 angstroms. the Pt. gp. metal is present as metal, the Sn is present in an oxidn. state above that of the metal, and the Co is present as metal and/or in state which is reducible to the metal under the conversion conditions. The pref. use is the reforming of a gasoline fraction to give a high octane reformate. Other conversions include (hydro)cracking, hydrogenolysis, (hydro)isomerisation, (de)hydrogenation, desulphurisation, cyclisation, polymerisation, alkylation, and de- and trans-alkylation.

VERFAHREN ZUR UMWANDLUNG EINES KOHLENWASSERSTOFFEINSATZMATERIALS

VERFAHREN ZUR UMWANDLUNG VON KOHLENWASSERSTOFFEN UND KATALYSATOR ZU SEINER DURCHFUEHRUNG

VERFAHREN ZUR HERSTELLUNG VON TONERDEEXTRUDATTEILCHEN UND DEREN VERWENDUNG

VERFAHREN UND KATALYSATOR ZUR UMWANDLUNG VON KOHLENWASSERSTOFFEN

Regeneration of catalysts - for hydrocarbon conversion by treatment with gaseous mixts contg oxygen,steam and halogen

Catalysts contg. a Pt gp. components, rhenium and a halogen component on a porous carrier, which have become deactivated by carbon deposits in use, are (a) treated at 350-500 degrees C with a mixt. consisting of 0.2-3 vol.% O2 0.02-25% H2O, 0.0005-5% halogen or halogen cpd and an inert gas until the carbon is substantially removed, (b) treated at 400-550 degrees C for 0.5-5 h with a mixt. consisting of 0.2-25 vol.% O2, 0.02-25% H2O 0.0005-5% of halogen or halogen cpd. and an inert gas (c) rinsed with inert gas to remove O2 and H2O and (d) heated in hydrogen for 0.5-5 h. at 370-600 degrees C. The catalysts are pref. those contg. 0.1-1.5 wt.% halogen (pref. Cl or F), 0.01-1.0 wt.% Pf-gp. metal (pref. Pf or Pd) and 0.01-1.0 wt.% Re, or an alumina carrier (pref. gamma or n-Al2O3). The process restores the catalyst to virtually the original activity and stability.

Patent FI753132A

POROESE HEAT RESISTANT INORGANIC OXIDE PARTICLES AND USES

Process for regenerating a deactivated hydrocarbon conversion catalyst.

Proces for the conversion of hydrocarbons

Patent FI51820B

Dehydrogenation catalyst

Controlling sulphur content in platinum-rhenium reforming

In the prepn. of gasoline by reforming over a catalyst comprising a Pt gp., a Re, an S, and a halogen component on an alumina carrier, the improvement comprises controlling the amount of S or S-contg. cpd. continuously fed to the reforming zone as a direct fraction of the atomic ratio of the Pt gp. metal to the Re in the catalyst.

Verfahren zur Herstellung eines Katalysators und dessen Verwendung

Verfahren zur Regenerierung eines entaktivierten Kohlenwasserstoffumwandlungskatalysators

Manufacture of chromia-alumina catalysts

Manufacture of chromia-alumina catalysts

Process for preparing alumina sol

Verfahren zur Herstellung von Metall Oxyd oder hydroxydsolen

Verfahren zur Herstellung von Tonerdeso)

Syart-up method foran lpg-reforming process

Process for preparing alumina sol

Kontinuierliches Verfahren zur Herstellung von Solen

Verfahren zur Herstellung von Chromoxyd-Aluminiumoxyd-Katalysatoren

Catalytic composite of platinum, tin and germanium with carrier material and reforming therewith

Catalytic composite of platinum, tin and germanium with carrier material and reforming therewith

Improved catalytic reforming

Verfahren zur herstellung von chromoxyd-aluminiumoxyd-katalysatoren

Regeneration of a coke deactivated catalyst containing platinum and rhenium

Regeneration of a coke deactivated catalyst containing platinum and rhenium