Texaco Inc.

Roy E Pratt

Gerald V Nelson

Leonce F Castagnos, Jr

Govanon Nongbri

Pei-Shing E Dai

David E Sherwood, Jr

Scott M Sayles

Richard P Scott, Deceased

Kerry W Bowers

William R Menzies, Iii

Hsu-Hui Hsing

Chi-Lin O'Young

John P MacLean

Chih-Hao Mark Tsang

Jitendra A Patel

Thomas A Lionetti

Charles H Schrader

MIchael P Bellinger

David E Self

William B Livingston

Edward W Dillingham

Joel S Bittensky

Howard C Kliesch

Donald H Schmude

Daniel N McWilliams

Joseph C Demeter

Heavy hydrocarbons are hydrotreated to increase content of components boiling below 1000.degree. F. by contact with Group VIII non-noble metal oxide and Group VI-B metal oxide on alumina having a Total Surface Area of 150-240 m.sup.2 /g, a Total Pore Volume, (TPV) of 0.7-0.98, and a Pore Diameter Distribution whereby .ltoreq.20% of the TPV is present as primary micropores of diameter .ltoreq.100 .ANG., at least about 34% of TPV is present as secondary micropores of diameter of about 100 .ANG.-200 .ANG., and about 26%-46% of the TPV is present as mesopores of diameter .gtoreq.200 .ANG..

Catalyst with specified pore size distribution

Heavy hydrocarbons are hydrotreated to increase content of components boiling below 1000.degree. F. by contact with Group VIII non-noble metal oxide and Group VIB metal oxide on alumina having a Total Surface Area of 175-220 m.sup.2 /g, a Total Pore Volume (TPV) of 0.6-0.8, and a Pore Diameter Distribution whereby .ltoreq.33% of the TPV is present as primary micropores of diameter .ltoreq.100 .ANG., at least about 41% of TPV is present as secondary micropores of diameter of about 100 .ANG.-200 .ANG., and about 16%-26% of the TPV is present as mesopores of diameter .gtoreq.200 .ANG.. Phosphorus containing compounds are avoided during catalyst preparation.

Catalyst for residual conversion demonstrating reduced toluene insolubles

Heavy hydrocarbons are hydrotreated to increase content of components boiling below 1000.degree. F. by contact with Group VIII non-noble metal oxide and Group VI-B metal oxide on alumina having a Total Surface Area of 150-240 m.sup.2 /g, a Total Pore Volume, (TPV) of 0.7-0.98, and a Pore Diameter Distribution whereby .ltoreq.20% of the TPV is present as primary micropores of diameter .ltoreq.100 .ANG., at least about 34% of TPV is present as secondary micropores of diameter of about 100 .ANG.-200 .ANG., and about 26%-46% of the TPV is present as mesopores of diameter &gt;200 .ANG..

Hydroconversion process employing catalyst with specified pore size

Heavy oils may be hydrotreated in the presence of a porous alumina support bearing metals of Group VIII and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 165-230 m.sup.2 /g, a Total Pore Volume of 0.5-0.8 cc.g, and a Pore Diameter Distribution whereby less than about 5% the Total Pore Volume is present as primary micropores of diameter less than 80 .ANG., and secondary micropores of diameter of +20 .ANG. of a Pore Mode of 100-135 .ANG. are present in amount of at least about 65% of the micropore volume having pores with diameter less than 250 .ANG., and 22-29% of the Total Pore Volume is present as macropores of diameter &gt;250 .ANG.. The process of the instant invention is particularly effective in achieving desired levels of hydrodemetallation, hydrodesulfurization, and hydrocracking of asphaltenes in the fraction of hydrotreated/hydrocracked petroleum resid product having a boiling point greater than 1000.degree. F.

Hydroconversion catalyst with specified pore size distribution

Heavy oils may be hydrotreated in the presence of a porous alumina support bearing metals of Group VIII and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 165-230 m.sup.2 /g, a Total Pore Volume of 0.5-0.8 cc.g, and a Pore Diameter Distribution whereby less than about 5% of the Total Pore Volume is present as primary micropores of diameter less than 80.ANG., and secondary micropores of diameter of .+-.20.ANG. of a Pore Mode of 100-135.ANG. are present in amount of at least about 65% of the micropore volume having pores with diameter less than 250.ANG., and 22-29% of the Total Pore Volume is present as macropores of diameter &gt;250.ANG.. The process of the instant invention is particularly effective in achieving desired levels of hydrodemetallation, hydrodesulfurization, and hydrocracking of asphaltenes in the fraction of hydrotreated/hydrocracked petroleum resid product having a boiling point greater than 1000.degree. F.

A hydrocarbon feedstock is catalytically cracked at an elevated temperature in a cracking zone with a zeolite cracking catalyst. The cracking catalyst employed comprises a crystalline aluminosilicate zeolite catalyst and a hybrid [Al,B]-zeolite catalyst. In this process the hydrocarbon feedstock is contacted with the zeolite catalyst in, for example, a fluidized bed catalytic cracking unit to yield cracked products containing increased amounts of C.sub.3 /C.sub.8 olefins.

Hydrocarbon cracking process employing zeolite catalysts with hybrid

A straight run naphtha is fractionated to yield on intermediate naphtha and the heaviest 10 vol % as heavy naphtha. The intermediate naphtha is catalytically reformed to yield reformed naphtha having a 90 vol % temperature (T90) of 310.degree. F. (155.degree. C.). The heavy naphtha is subjected to fluid catalytic cracking (FCC) to yield liquid fuel and lighter, including C.sub.4 olefins and a cracked naphtha having a research octane number suitable for gasoline blending.

Heavy naphtha conversion process

In a two stage catalytic cracking process a heavy cycle gas oil fraction (HCGO) nominal boiling range 600.degree. F. to 1050.degree. F., API gravity of -10.degree. to +10.degree. and 65 to 95 vol % aromatics is recycled to extinction between an ebullated bed hydrocracking zone and fluidized catalytic cracking zone to yield a liquid fuel and lighter boiling range fraction as the light fraction from each zone. The catalyst in the fluidized catalytic cracking zone is maintained at a micro activity 68 to 72 while cracking a virgin gas oil to HCGO. HCGO is then mixed with vacuum residuum and hydrocracked in an ebullated bed reactor. The mid range fraction is recycled to the fluidized catalytic cracking zone. The 1000.degree. F..sup.+ fraction is blended with a fuel oil.

Two catalyst stage hydrocarbon cracking process

In an ebullated bed process, a residual hydrocarbon oil and a hydrogen containing gas is passed upwardly through an ebullated bed of catalyst in a hydrocracking zone at a temperature in the range of 650.degree. F. to 950.degree. F. and pressure of 1000 psia to 5000 psia. The hydrogen containing gas comprises hydrogen sulfide in an amount to maintain the sulfur content of the oil in the hydrocracking zone at 2 wt % to 10 wt %. A hydrocracked oil is recovered characterized by having a reduced sediment content.

Suppressing sediment formation in an ebullated bed process

SO.sub.x in regenerator off gas in a fluid cracking unit is decreased by providing in the regenerator bed, a metal grid bearing a layer of rare earth oxide.

Reduction of SO.sub.x in regenerator off gas of a fluid cracking unit

Apparatus for catalytic cracking of a selected portion of a hydrocarbon feedstock comprising a riser reactor and a catalyst regenerator, a regenerated catalyst cooler, and an absorber. Regenerated catalyst from the catalyst regenerator is conducted through the catalyst cooler into the absorber where it adsorbs hydrocarbon cracking feedstock and then returned to the riser reactor. A duct carries part of the hot regenerated catalyst from the catalyst regenerator directly to the riser reactor to supply heat for cracking the hydrocarbon feedstock.

Fluid catalytic cracking apparatus

An improved method for fluidized catalytic cracking of a selected portion of a paraffinic hydrocarbon feedstock in which a paraffinic chargestock for a fluid catalytic cracking unit is processed for the separation of at least a part of its paraffinic components from non-paraffins by means of a zeolite composition which acts both as a molecular sieve and a cracking catalyst. The paraffins-containing fraction adsorbed on the molecular sieve is subjected to catalytic cracking in a riser-type fluid catalytic cracking reaction zone at a temperature in the range of 650.degree. to 700.degree. C. under subatmospheric pressure conditions for the production of light olefins.

Fluid catalytic cracking method

An improved air distribution apparatus for a regenerator in a fluid catalytic cracking process has been invented. The improvement is in the nozzles which eject air from an air ring to a bed of coke deactivated catalyst. The nozzles are positioned to take air from the centerline of the air ring and are of length 4 to 8 diameters. The nozzles are noted for reduced aspirated catalyst erosion.

Air distribution apparatus for a fluid catalytic cracking catalyst

A method and apparatus for regeneration of coked catalyst resulting from a hydrocarbon conversion reaction in which catalyst regeneration is carried out in a plurality of superposed regeneration zones comprising the combination of a first dense phase fluidized bed regeneration zone, an entrained catalyst dilute phase regeneration zone superposed on said first regeneration zone, and a second dense phase fluid bed regeneration zone superposed on said dilute phase regeneration zone. Catalyst is regenerated by combustion of coke from the surface of the catalyst at an elevated temperature in the range of 675.degree. to 800.degree. C. with an excess of oxygen supplied by an oxygen-containing regeneration gas part of which is introduced into the first fluidized bed regeneration zone and part into said dilute phase regeneration zone, including a novel means of control of the rate of catalyst recirculated from said second dense phase regeneration zone to said first regeneration zone.

Regeneration of fluidizable catalyst

A method and apparatus for catalytic conversion of hydrocarbon feedstocks and regeneration of coked catalyst resulting from the hydrocarbon conversion reaction in which the catalyst regeneration is carried out in a combination of dense phase fluidized bed, an entrained phase regeneration zone and a second dense phase fluidized bed and the hydrocarbon conversion reaction is carried out in a high velocity short contact time dilute phase reaction zone wherein the reaction time and temperature and the regenerator temperature may be separately varied to provide and maintain optimum conversion conditions.

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Port Neches, TX, United States of America

Roy E Pratt