US 4,169,040 AGranted

Staged process for the production of middle distillate from a heavy distillate

AssigneeChevron Research Company

InventorsDonald A. Bea, Joseph Jaffe

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Abstract

Middle distillate oil is produced with a minimum production of lighter hydrocarbons by (1) contacting hydrogen gas and a heavy distillate oil containing nitrogenous hydrocarbons with a catalyst in a first reaction zone under selected conditions, and (2) contacting hydrogen gas and at least a portion of the resulting effluent from the first zone with a catalyst in a second reaction zone under selected conditions. In each zone the catalyst is a composite of an amorphous silica-alumina carrier and a hydrogenation component wherein the silica and hydrogenation component are highly dispersed.

Claims14

Dependent claims

A process for producing middle distillate from a heavy distillate feed having a boiling point range in the normal boiling point range above 343.degree. C. and a nitrogenous hydrocarbon content, calculated as nitrogen, of at least 100 ppmw, the steps comprising:

(1) contacting in a first reaction zone said feed and hydrogen gas with a catalyst under conditions including:
(a) a temperature below about 454.degree. C. (850.degree. F.);
(b) a hydrogen partial pressure above about 69 atmospheres (1000 psig);
(c) a hydrogen gas-to-feed ratio in the range of from about 0.356 to 3.56 SCM/L (2,000-20,000 SCF/BBL);
and
(d) a liquid hourly space velocity in the range of from about 0.1 to 5 V/V/Hr.;
said conditions being selected to produce a first reaction zone effluent containing a first liquid hydrocarbon phase having (i) a nitrogenous hydrocarbon content, calculated as nitrogen, above about 1 ppmw and less than one-half of that of said feed, and (ii) a content of product resulting from said contacting boiling in the range below about 371.degree. C. (700.degree. F.) of less than about 50 volume percent of said feed;
(2) passing said first reaction zone effluent and admixed water into a first high-pressure separation zone;
(3) withdrawing from said first separation zone a first intermediate liquid hydrocarbon phase, a first liquid foul-water phase, and a first gas comprising hydrogen;
(4) contacting a bottoms feed and hydrogen gas with a catalyst in a second reaction zone under conditions, including:
(a) a temperature below about 454.degree. C. (850.degree. F.);
(b) a hydrogen partial pressure above about 69 atmospheres (1000 psig);
(c) a hydrogen gas-to-feed ratio in the range of from about 0.356 to 3.56 SCM/L (2,000-20,000 SCF/BBL);
and
(d) a liquid hourly space velocity in the range of from about 1 to 20 V/V/Hr.;
said conditions being selected to produce a second reaction zone effluent containing, based upon said bottoms feed, an amount of hydrocarbons boiling below about 371.degree. C. (700.degree. F.) in the range of from about 40 to 70 volume percent;
(5) passing said second reaction zone effluent and admixed water into a second high-pressure separation zone;
(6) withdrawing from said second separation zone a second intermediate liquid hydrocarbon phase, a second liquid foul-water phase, and a second gas comprising hydrogen;
(7) passing said first and second intermediate liquid hydrocarbon phases into a low-pressure separation zone;
(8) withdrawing from said low-pressure separation zone a second liquid hydrocarbon phase, a third liquid foul-water phase, and a gas comprising light hydrocarbons;
(9) separating said second hydrocarbon phase into at least two fractions, including:
(a) an overhead middle distillate fraction boiling in the range of from about 127.degree. C. (260.degree. F.) to 371.degree. C. (700.degree. F.);
and
(b) a bottoms fraction boiling in the range above about 371.degree. C. (700.degree. F.), said bottoms fraction, at least in part, being used as said bottoms feed;
and wherein said catalysts for said zones are selected from the group consisting of catalysts consisting essentially of an amorphous silica-alumina carrier component containing for each part by weight of silica an amount of alumina in the range of from about 0.6 to 4 parts, and at least one hydrogenation component selected from the group consisting of the metals, oxides and sulfides of nickel, cobalt, molybdenum and tungsten, said catalyst containing for each 100 parts by weight an amount, calculated as metal, of said hydrogenation component in the range of from about 1 to 50 parts, said silica and said hydrogenation components, in terms of electron microprobe composition scan of said catalyst, having standard deviations in their respective concentrations around the mean thereof, which is less than about 25 percent.

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A process for converting a heavy hydrocarbon distillate feedstock boiling above 343.degree. C. and containing more than 100 ppmw organic nitrogen in high yield to a middle distillate product boiling in the range 127.degree.-371.degree. C. which comprises:

(1) hydrocracking and hydrofining said feedstock in a first reaction zone at a hydrocracking conversion of less than 50 volume percent to products boiling below 343.degree. C. and at a hydrofining conversion of said organic nitrogen of at least 50 weight percent, said hydrofining and hydrocracking being conducted in the presence of a catalyst and 2000-70,000 SCF of hydrogen per barrel of said feedstock at conditions including a temperature below 850.degree. F., a hydrogen partial pressure above 1000 psig, and a liquid hourly space velocity of 0.1-5 V/V/hr.;
(2) withdrawing a reaction product effluent from said reaction zone forming a mixture of said effluent with water, removing from said mixture light gases including hydrogen, hydrogen sulfide and light hydrocarbon gases, and further removing from said mixture foul water containing ammonia, to produce a remaining reaction product comprising light hydrocarbons, middle distillate hydrocarbons in substantial quantities and heavier hydrocarbons boiling above 371.degree. C.;
(3) hydrocracking said heavier hydrocarbons in a second reaction zone at a hydrocracking conversion of 40-70 volume percent to products boiling below 371.degree. C., in the presence of a catalyst and 2000-20,000 SCF per barrel of said heavier hydrocarbons at conditions including a temperature below 850.degree. F., a hydrogen partial pressure above 1000 psig, and a liquid hourly space velocity of 1-20 V/V/hr.;
(4) withdrawing a reaction product effluent from said second reaction zone, forming a mixture of said effluent with water, removing from said mixture light gases including hydrogen, hydrogen sulfide and light hydrocarbon gases, and further removing from said mixture foul water containing ammonia, to produce a remaining reaction product comprising light hydrocarbons, and middle distillate hydrocarbons in substantial quantities;
said catalysts in each of said first and second reaction zones being selected from the group consisting of catalysts consisting essentially of an amorphous silica-alumina carrier component containing for each part by weight of silica an amount of alumina in the range of from about 0.6 to 4 parts, and at least one hydrogenation component selected from the group consisting of the metals, oxides and sulfides of nickel, cobalt, molybdenum and tungsten, said catalyst containing for each 100 parts by weight an amount, calculated as metal, of said hydrogenation component in the range of from about 1 to 50 parts, said silica and said hydrogenation components, in terms of electron microprobe composition scan of said catalyst, having standard deviations in their respective concentrations around the mean thereof, which is less than about 25 percent.

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Dependencies are inferred from the claim text.

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Abstract

(1) contacting in a first reaction zone said feed and hydrogen gas with a catalyst under conditions including:
(a) a temperature below about 454.degree. C. (850.degree. F.);
(b) a hydrogen partial pressure above about 69 atmospheres (1000 psig);
(c) a hydrogen gas-to-feed ratio in the range of from about 0.356 to 3.56 SCM/L (2,000-20,000 SCF/BBL);
and
(d) a liquid hourly space velocity in the range of from about 0.1 to 5 V/V/Hr.;
said conditions being selected to produce a first reaction zone effluent containing a first liquid hydrocarbon phase having (i) a nitrogenous hydrocarbon content, calculated as nitrogen, above about 1 ppmw and less than one-half of that of said feed, and (ii) a content of product resulting from said contacting boiling in the range below about 371.degree. C. (700.degree. F.) of less than about 50 volume percent of said feed;
(2) passing said first reaction zone effluent and admixed water into a first high-pressure separation zone;
(3) withdrawing from said first separation zone a first intermediate liquid hydrocarbon phase, a first liquid foul-water phase, and a first gas comprising hydrogen;
(4) contacting a bottoms feed and hydrogen gas with a catalyst in a second reaction zone under conditions, including:
(a) a temperature below about 454.degree. C. (850.degree. F.);
(b) a hydrogen partial pressure above about 69 atmospheres (1000 psig);
(c) a hydrogen gas-to-feed ratio in the range of from about 0.356 to 3.56 SCM/L (2,000-20,000 SCF/BBL);
and
(d) a liquid hourly space velocity in the range of from about 1 to 20 V/V/Hr.;
said conditions being selected to produce a second reaction zone effluent containing, based upon said bottoms feed, an amount of hydrocarbons boiling below about 371.degree. C. (700.degree. F.) in the range of from about 40 to 70 volume percent;
(5) passing said second reaction zone effluent and admixed water into a second high-pressure separation zone;
(6) withdrawing from said second separation zone a second intermediate liquid hydrocarbon phase, a second liquid foul-water phase, and a second gas comprising hydrogen;
(7) passing said first and second intermediate liquid hydrocarbon phases into a low-pressure separation zone;
(8) withdrawing from said low-pressure separation zone a second liquid hydrocarbon phase, a third liquid foul-water phase, and a gas comprising light hydrocarbons;
(9) separating said second hydrocarbon phase into at least two fractions, including:
(a) an overhead middle distillate fraction boiling in the range of from about 127.degree. C. (260.degree. F.) to 371.degree. C. (700.degree. F.);
and
(b) a bottoms fraction boiling in the range above about 371.degree. C. (700.degree. F.), said bottoms fraction, at least in part, being used as said bottoms feed;
and wherein said catalysts for said zones are selected from the group consisting of catalysts consisting essentially of an amorphous silica-alumina carrier component containing for each part by weight of silica an amount of alumina in the range of from about 0.6 to 4 parts, and at least one hydrogenation component selected from the group consisting of the metals, oxides and sulfides of nickel, cobalt, molybdenum and tungsten, said catalyst containing for each 100 parts by weight an amount, calculated as metal, of said hydrogenation component in the range of from about 1 to 50 parts, said silica and said hydrogenation components, in terms of electron microprobe composition scan of said catalyst, having standard deviations in their respective concentrations around the mean thereof, which is less than about 25 percent.

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