Exxon Research and Engineering Company

Other

Willard H Sawyer

Neville L Cull

Glen P Hamner

Howard L Mitchell, Iii

Glen P Hamner, Deceased

William F Arey, Jr

Ian A Cody

William E Winter, Jr

Carl W Hudson

Fred M Long

Roby Bearden, Jr

Russell R Chianelli

James J Schorfheide

Francis X Mayer

James H Taylor, Jr

Harry E Robson

Robert H Waghorne

Heather A Boucher

David E Mueller

Hamner, Deceased Glen P

Davis S Mark

Michael T Duncan

A slurry hydrotreating process is described in which a hydrotreating catalyst of small particle size is contacted with a heavy fossil fuel. High catalyst activity is maintained by circulating the catalyst between a hydrotreating zone and a reactivating zone where the catalyst is hydrogen stripped.

Slurry hydrotreating process

A wax isomerization catalyst is described which comprises a Group VIII hydrogenation metal component on fluorided alumina or material containing alumina which catalyst possesses a surface nitrogen content N/Al ratio of about 0.01 or less determined by X-ray photoelectron spectroscopy, a bulk fluorine content of between about 2 to 10 wt %, a surface fluorine content defined as the amount of fluorine in a layer extending from the outer surface to a depth of about 1/100 of an inch of less than about 3 wt % provided that the surface fluoride concentration is less than the bulk fluoride concentration and an aluminum fluoride hydroxide hydrate peak height of 60 or less determined as the relative amount of hydrate represented by a peak in the X-ray diffraction pattern at 2.theta.=5.66 .ANG. when a hydrate level of 100 corresponds to the XRD peak height exhibited by a standard material. Also described is a method for producing a slack wax isomerization catalyst said method comprising depositing a Group VIII hydrogenation metal on alumina or material containing alumina extrudate, calcining said metal loaded extrudate, fluoriding said material using an aqueous fluorine source solution having a pH of 3.5 to 4.5 to a bulk fluorine level of about 8 wt % or less followed by heating in an air oxygen containing atmosphere or inert gas from ambient to 350.degree. to 450.degree. C. within 3 hours and holding at the final temperature, if necessary, for a time sufficient to reduce the hydrate and nitrogen contents to the aforesaid levels. Alternatively the catalyst can be made using a fluorine solution of pH less than 3.5 to a bulk fluorine level of about 10 wt % or less followed by heating in air or an oxygen containing atmosphere, or inert atmosphere at about 350.degree. to 450.degree. C.

Wax isomerization catalyst and method for its production

A novel slurry hydrotreating process is described which employs a hydrotreating catalyst of small particle size having a quantity of catalyst sites in excess of those required for reaction and/or adsorption of nitrogen compounds in the petroleum or synfuel feed being treated. The excess catalyst sites can therefore in effect be contacted with a low nitrogen or essentially zero nitrogen feed, allowing rapid hydrogenation of aromatics at low temperatures where equilibrium is favored. In a further aspect of the invention, the catalyst which contains adsorbed nitrogen is activated by high temperature denitrogenation.

Slurry hydroprocessing process

A fluorided platinum-on-alumina catalyst for wax isomerization wherein the platinum is substantially uniformly distributed throughout the catalyst in the form of relatively small crystallites, of the total fluoride present in the catalyst very little is located on the outer surface of the catalyst and a significant concentration of the fluoride within the catalyst is present as aluminum fluoride hydroxide hydrate. The catalyst is prepared by contacting a platinum-on-alumina with a solution having a relatively high concentration of fluoride and drying the fluorided platinum-on-alumina catalyst at temperatures not in excess of 650.degree. F.

Catalyst for the hydroisomerization and hydrocracking of waxes to

A process for selectively producing middle distillate fuel products from paraffin waxes such as slack wax and Fischer-Tropsch wax by hydroisomerizing the wax to convert 60-95 weight percent per pass of the 700.degree. F..sup.+ fraction contained in said wax. The catalyst employed is a fluorided Group VIII metal-on-alumina catalyst where the fluoride within the catalyst is present predominately as aluminum fluoride hydroxide hydrate. The preferred Group VIII metal is platinum.

Process for the hydroisomerization of was to produce middle distillate

An improved wax isomerization catalyst is described which is a hydrogenation metal on halogenated refractory metal oxide support catalyst characterized in that the catalyst is prepared by depositing the hydrogenation metal on the refractory metal oxide support followed by fluoriding using a low pH fluorine source such as aqueous HF. Thereafter the catalyst is crushed to expose inner surfaces, the crushed catalyst being sieved to remove fines, the catalyst charge having an average particle diameter of 1/32 inch and smaller across the longest continuous cross sectional dimension, preferably between 1/64 to 1/32'. Alternatively, the catalyst is made by depositing a hydrogenation metal on a refractory metal support, crushing the material to a particle size of 1/32 inch and smaller across the longest continuous cross-sectional dimension and fluoriding said material using acidic fluorine source such as HF. Following sizing the sized catalyst is activated by heating in a hydrogen atmosphere. Isomerization using this 'sized' catalyst is marked by the production of an isomerized dewaxed oil product having unexpectedly high VI and superior levels of selective conversion of wax to liquid isomerized product.

Method for producing a wax isomerization catalyst

A process for the production of high octane gasoline, or high octane gasoline blending components, from a sulfur-containing feed rich in fused two-ring aromatic hydrocarbons, inclusive of naphthalenes. The feed is hydrogenated in a first reaction zone to desulfurize the feed and saturate one ring of the fused two-ring aromatic hydrocarbons, but insufficient to saturate the second ring of said molecular species, to form tetralins. The product, as a feed, is reacted in a second reaction zone over a catalyst comprised of elemental iron and one or more alkali or alkaline-earth metals components to selectively hydrogenate and crack the previously hydrogenated fused two-ring aromatic hydrocarbons to produce lower molecular weight higher octane components suitable per se as gasoline, or gasoline blending components. The feed rich in fused two-ring aromatic hydrocarbons can be split from a wider boiling range hydrocarbon to obtain, additionally, a component rich in fused multi-ring aromatic hydrocarbons having three or more rings to the molecule, which fraction can also be hydrogenated to produce other fuels, or raw materials feed components.

Process for the production of ultra high octane gasoline, and other

A process for the production of high octane gasoline, or high octane gasoline blending components from a sulfur and nitrogen-containing feed composition of wide boiling range rich in fused multi-ring aromatic hydrocarbons containing two, and three or more rings in the molecule. The feed is first hydrogenated to desulfurize, denitrogenate and saturate one ring of the two-ring molecular species, but insufficient to saturate the second ring of said molecular species. The product, as a feed, is then hydrocracked to crack fused multi-ring aromatic hydrocarbons containing three or more rings to the molecule, and to produce lower molecular weight, lower boiling components. The product of the hydrocracker is then split into blends which include (i) a blend rich in fused two-ring aromatic hydrocarbons and (ii) a blend rich in fused multi-ring aromatic hydrocarbons containing three or more rings to the molecule. Blend (i) is selectively hydrogenated and cracked over a catalyst comprised of elemental iron and one or more alkali or alkaline-earth metals to produce gasoline or gasoline blending components, and blend (ii) is hydrocracked to produce gasoline or gasoline blending components.

A process for the preparation of novel highly active, highly selective hydrotreating catalysts. These catalysts are prepared, in bulk or in supported form, from a catalyst precursor characterized by the formula B.sub.x [Mo.sub.3 S.sub.z ] where B is an ammonium ion, polyammonium ion, tertiary or quaternary phosphonium ion, or a hydrocarbyl substituted ammonium ion, hydrocarbyl substituted polyammonium ion, or hydrocarbyl substituted tertiary or quaternary phosphonium ion, x is 1 where B is a divalent cationic moiety, or 2 where B is a monovalent cationic moiety, [Mo.sub.3 S.sub.z ] is a divalent anionic moiety wherein z is an integer greater than 15. The catalyst precursor is dispersed in an ammonium sulfide or dilute ammonium polysulfide solution and heated to remove sulfur from said catalyst precursor to provide a z value of 15 or less. Carbon is also removed from the catalyst precursor and, where B of the B.sub.x [Mo.sub.3 S.sub.z ] catalyst precursor is a non-carbon containing moiety, the finished catalyst will contain an atomic ratio of C/Mo of less than about 0.05. Decomposition of the catalyst precursor in the presence of hydrogen, hydrocarbon and sulfur forms the highly active hydrotreating catalyst.

Catalysts from molybdenum polysulfide precursors, their preparation and

A process for the preparation of novel highly active, highly selective hydrotreating catalysts. These catalysts are prepared, in bulk or in supported form, by contacting together and decomposing, in the presence of hydrogen, hydrocarbon, and sulfur, a catalyst precursor characterized by the formula B.sub.x [Mo.sub.3 S.sub.z ] where B is an ammonium ion, polyammonium ion, tertiary or quaternary phosphonium ion, or a hydrocarbyl substituted ammonium ion, hydrocarbyl substituted polyammonium ion, or hydrocarbyl substituted tertiary or quaternary phosphonium ion, x is 1 where B is a divalent cationic moiety, or 2 where B is a monovalent cationic moiety, [Mo.sub.3 S.sub.z ] is a divalent anionic moiety wherein z is an integer ranging from about 10 to about 46. A preferred precursor catalyst species is Mo.sub.3 (S.sub.2).sub.6 S.

Catalysts from molybdenum polysulfide precursors and their preparation

A catalyst comprising Group VIB and Group VIII metal components and a support prepared by treating alpha alumina monohydrate with an acid solution comprising a hydrolyzable metal salt, such as zirconium nitrate.

Hydroprocessing catalysts

A catalyst is provided which comprises an ultrastable Y-type crystalline aluminosilicate zeolite, an alumina-aluminum fluorophosphate and a hydrogenation component. Hydrocarbon hydroprocessing processes utilizing the catalyst are also provided.

Hydrocracking over alumina-aluminum fluorophosphate-containing catalysts

A catalyst is provided which comprises a hydrogenation component and a support comprising agglomerates of alumina having initially not more than 0.20 cubic centimeters per gram of its pore volume in pores greater than about 400 Angstroms in diameter and a minor amount of silica. A process for the hydroconversion of hydrocarbonaceous oils utilizing the catalyst is also provided.

Growing community of inventors

Baton Rouge, LA, United States of America

Willard H Sawyer