HYDROPROCESSING THERMALLY CRACKED PRODUCTS

Embodiments herein relate to a process flow scheme for the processing of gas oils and especially reactive gas oils produced by thermal cracking of residua using a split flow concept. The split flow concepts disclosed allow optimization of the hydrocracking reactor severities and thereby take advantage of the different reactivities of thermally cracked gas oils versus those of virgin gas oils. This results in a lower cost facility for producing base oils as well as diesel, kerosene and gasoline fuels while achieving high conversions and high catalyst lives. 114-. (canceled)15. A system for upgrading gas oils to distillate hydrocarbons , the system comprising:a flow control system for dividing a first gas oil stream into a first and second portions;a mixing device for mixing a second gas oil stream and the first portion of the first gas oil stream to form a mixed gas oil stream;a first hydrocracker reaction system for contacting the mixed gas oil stream and hydrogen with a first hydroconversion catalyst to convert at least a portion of the hydrocarbons in the mixed gas oil stream to distillate hydrocarbons;a separation system for fractionating an effluent from the first hydrocracker reaction system into one or more hydrocarbon fractions including a fraction comprising the unconverted hydrocarbons;a second hydrocracker reaction system for contacting hydrogen and the fraction comprising the unconverted hydrocarbons with a second hydroconversion catalyst to convert at least a portion of the hydrocarbons in the mixed gas oil stream to distillate hydrocarbons;a flow line for feeding the effluent from the second hydrocracking reaction system to the fractionating system for concurrent fractionation with the effluent from the first hydrocracker reaction system;a third hydrocracker reaction system for contacting hydrogen and the second portion of the first gas oil stream with a third hydroconversion catalyst to convert at least a portion of the hydrocarbons in the second ...

Method for making middle distillates and a heavy vacuum gas oil FCC feedstock

The present invention is directed to a refining process for producing hydroprocessed distillates and a heavy vacuum gas oil (HVGO). The process produces middle distillates that have reduced nitrogen and sulfur content, while simultaneously producing a 900° F. + (482° C. + ) HVGO stream useful as a fluidized catalytic cracking (FCC) unit feedstock.

Conversion of asphaltenic pitch within an ebullated bed residuum hydrocracking process

A process for upgrading residuum hydrocarbons including: feeding pitch, hydrogen, and a partially spent catalyst recovered from a hydrocracking reactor to an ebullated bed pitch hydrocracking reactor; contacting the pitch, hydrogen, and the catalyst in the ebullated bed pitch hydrocracking reactor at reaction conditions of temperature and pressure sufficient to convert at least a portion of the pitch to distillate hydrocarbons; and separating the distillate hydrocarbons from the catalyst. In some embodiments, the process may include selecting the ebullated bed pitch hydrocracking reactor reaction conditions to be at or below the level where sediment formation would otherwise become excessive and prevent continuity of operations.

Upgrading raw shale-derived crude oils to hydrocarbon distillate fuels

Integrated processes for upgrading crude shale-derived oils, such as those produced by oil shale retorting or by in situ extraction or combinations thereof. Processes disclosed provide for a split-flow processing scheme to upgrade whole shale oil. The split flow concepts described herein, i.e., naphtha and kerosene hydrotreating in one or more stages and gas oil hydrotreating in one or more stages, requires additional equipment as compared to the alternative approach of whole oil hydrotreating. While contrary to conventional wisdom as requiring more capital equipment to achieve the same final product specifications, the operating efficiency vis a vis on-stream time efficiency and product quality resulting from the split flow concept far exceed in value the somewhat incrementally higher capital expenditure costs.

Hydroprocessing thermally cracked products

Embodiments herein relate to a process flow scheme for the processing of gas oils and especially reactive gas oils produced by thermal cracking of residua using a split flow concept. The split flow concepts disclosed allow optimization of the hydrocracking reactor seventies and thereby take advantage of the different reactivities of thermally cracked gas oils versus those of virgin gas oils. This results in a lower cost facility for producing base oils as well as diesel, kerosene and gasoline fuels while achieving high conversions and high catalyst lives.

Conversion of triacylglycerides-containing oils

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include reacting a triacylglycerides-containing oil-carbon dioxide mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides to a hydrocarbon or mixture of hydrocarbons comprising one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics.

Integration of residue hydrocracking and hydrotreating

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system.

System and process for producing linear alpha olefins

Processes and systems for producing linear alpha olefins are described herein. One embodiment is a process comprising: a) separating a mixed butene stream comprising 1 -butene and 2-butene into an overhead 1 -butene stream and a bottoms 2-butene stream in a butene distillation column, a portion of the bottoms 2-butene stream being separated to form a butene reboiler stream that is heated and vaporized in a reboiler and returned to the butene distillation column, (b) subjecting at least a portion of the overhead 1 -butene stream from (a) to catalytic metathesis to produce an effluent including 3-hexene, (c) isomerizing 3-hexene from (b) to produce a mixed hexene stream comprising 1 -hexene, 2-hexene and 3-hexene, (d); separating the mixed hexene stream in a hexene fractionation tower to form a 1 -hexene vapor overhead stream that is condensed in a cooler and a bottoms stream comprising 2-hexene and 3-hexene, and (e) using heat obtained by condensing the 1 -hexene vapor overhead stream of ...

Conversion of alcohols to distillate fuels

A process for the production of jet and other heavy fuels from alcohols and mixture of alcohols is disclosed. The process may include contacting in a reaction zone at least one C2 to C11 alcohol with a solid catalyst having activity for the simultaneous dehydration of the alcohols to form olefins, isomerization of the olefins to form internal olefins, and oligomerization of the olefins produced in situ via the dehydration reaction to form an effluent comprising mono-olefinic hydrocarbons. Preferably, the alcohol feed is a mixture of alcohols, such as C2 to C7 alcohols or C4 and C6 alcohols, enabling the production of a mixture of branched hydrocarbons that may be used directly as a jet fuel without blending.

Process for producing distillate fuels and anode grade coke from vacuum resid

A process for upgrading residuum hydrocarbon feedstocks that may include: contacting a residuum hydrocarbon and hydrogen with a hydroconversion catalyst in a residuum hydroconversion reactor system; recovering an effluent from the residuum hydroconversion reactor system; separating the effluent to recover two or more hydrocarbon fractions including at least a vacuum residuum fraction and a heavy vacuum gas oil fraction; combining at least a portion of the heavy vacuum gas oil fraction and at least a portion of the vacuum residuum fraction to form a mixed heavy hydrocarbon fraction; feeding at least a portion of the mixed heavy hydrocarbon fraction to a coker; operating the coker at conditions to produce anode grade green coke and distillate hydrocarbons; recovering the distillate hydrocarbons from the coker; fractionating the distillate hydrocarbons to recover hydrocarbon fractions including a light distillates fraction, a heavy coker gas oil fraction, and a coker recycle fraction.

Integration of residue hydrocracking and hydrotreating

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system.

PROCESS TO UPGRADE PARTIALLY CONVERTED VACUUM RESIDUA

Processes for upgrading partially converted vacuum residua hydrocarbon feeds are disclosed. The upgrading processes may include: steam stripping the partially converted vacuum residua to generate a first distillate and a first residuum; solvent deasphalting the first residuum stream to generate a deasphalted oil and an asphaltenes fraction; vacuum fractionating the deasphalted oil to recover a deasphalted gas oil distillate and a heavy deasphalted residuum; contacting the first distillate and the deasphalted gas oil distillate and hydrogen in the presence of a first hydroconversion catalyst to produce a product; contacting the heavy deasphalted residuum stream and hydrogen in the presence of a second hydroconversion catalyst to produce an effluent; and fractionating the effluent to recover a hydrocracked atmospheric residua and a hydrocracked atmospheric distillate

Process to upgrade partially converted vacuum residua

Processes for upgrading partially converted vacuum residua hydrocarbon feeds are disclosed. The upgrading processes may include: steam stripping the partially converted vacuum residua to generate a first distillate and a first residuum; solvent deasphalting the first residuum stream to generate a deasphalted oil and an asphaltenes fraction; vacuum fractionating the deasphalted oil to recover a deasphalted gas oil distillate and a heavy deasphalted residuum; contacting the first distillate and the deasphalted gas oil distillate and hydrogen in the presence of a first hydroconversion catalyst to produce a product; contacting the heavy deasphalted residuum stream and hydrogen in the presence of a second hydroconversion catalyst to produce an effluent; and fractionating the effluent to recover a hydrocracked atmospheric residua and a hydrocracked atmospheric distillate

Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization

A process for the double-bond isomerization of olefins is disclosed. The process may include contacting a fluid stream comprising olefins with a fixed bed comprising an activated basic metal oxide isomerization catalyst to convert at least a portion of the olefin to its isomer. The isomerization catalysts disclosed herein may have a reduced cycle to cycle deactivation as compared to conventional catalysts, thus maintaining higher activity over the complete catalyst life cycle.

CONVERSION OF TRIACYLGLYCERIDES-CONTAINING OILS TO HYDROCARBONS

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include: reacting a triacylglycerides-containing oil-water-hydrogen mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides and recovering a reaction effluent comprising water and one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics; hydrotreating the reaction effluent to form a hydrotreated effluent. 1. A process for converting triacylglycerides-containing oils into crude oil precursors and/ordistillate hydrocarbon fuels, the process comprising:reacting a triacylglycerides-containing oil-water-hydrogen mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides and recovering a reaction effluent comprising water and one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics;hydrotreating the reaction effluent to form a hydrotreated effluent.2. The process of claim 1 , further comprising mixing a triacylglycerides-containing oil with water and hydrogen to form the triacylglycerides-containing oil-water-hydrogen mixture.3. The process of claim 1 , further comprising mixing a triacylglycerides-containing oil with water to form a triacylglyceride-containing oil-water mixture.4. The process of claim 3 , further comprising mixing the triacylglyceride-containing oil-water mixture with hydrogen to form the triacylglyceride-containing oil-water-hydrogen mixture.5. The process of claim 1 , wherein the triacylglycerides-containing oil-water-hydrogen mixture has a water to triacylglycerides mass ratio in the range from about 0.001:1 to about 1:1.6. The process of claim 1 , wherein the triacylglycerides-containing oil-water-hydrogen mixture has a ...

CONVERSION OF ALCOHOLS TO DISTILLATE FUELS

A process for the production of jet and other heavy fuels from alcohols and mixture of alcohols is disclosed. The process may include contacting in a reaction zone at least one C2 to C11 alcohol with a solid catalyst having activity for the simultaneous dehydration of the alcohols to form olefins, isomerization of the olefins to form internal olefins, and oligomerization of the olefins produced in situ via the dehydration reaction to form an effluent comprising mono-olefinic hydrocarbons. Preferably, the alcohol feed is a mixture of alcohols, such as C2 to C7 alcohols or C4 and C6 alcohols, enabling the production of a mixture of branched hydrocarbons that may be used directly as a jet fuel without blending. 1. A process for the production of distillate fuels , the process comprising: i. dehydration of the alcohols to form olefins and water;', 'ii. oligomerization of the olefins produced in situ via the dehydration reaction; and', 'iii. isomerization of the resulting olefinic oligomers and olefins to form internal olefins,, 'contacting in a reaction zone a mixture of two or more C2 to C11 alcohols, including at least one secondary alcohol, with a solid catalyst having activity for the simultaneousto form an effluent comprising mono-olefinic hydrocarbon oligomers.2. The process of claim 1 , further comprising separating the mono-olefinic hydrocarbon oligomers from water claim 1 , any unreacted alcohols claim 1 , and any unreacted olefins.3. The process of claim 2 , further comprising recycling at least one of the unreacted alcohols and the unreacted olefins to the reaction zone.4. The process of claim 1 , further comprising hydrogenating the mono-olefinic hydrocarbon oligomers to produce a paraffinic hydrocarbon product.5. The process of claim 4 , further comprising fractionating the paraffinic hydrocarbon product into one or more hydrocarbon fractions useful as a fuel or a fuel blendstock.6. The process of claim 5 , wherein the one or more hydrocarbon fractions are ...

CONVERSION OF TRIACYLGLYCERIDES-CONTAINING OILS TO HYDROCARBONS

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include: reacting a triacylglycerides-containing oil-water-hydrogen mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides and recovering a reaction effluent comprising water and one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics; hydrotreating the reaction effluent to form a hydrotreated effluent. 1. A system for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels , the system comprising:a mixing device for mixing a triacylglycerides-containing oil feed with water to form an oil-water mixture;a mixing device for mixing the oil-water mixture with hydrogen to form a feed mixture;a hydrothermolysis reactor for reacting the feed mixture at a temperature in the range of 250° C. to about 525° C. and a pressure greater than about 75 bar to produce a reaction effluent;a hydrotreater for hydrotreating the reaction effluent;a separator for separating water and hydrogen from hydrocarbons in the hydrotreated effluent.2. The system of claim 1 , further comprising one or more fluid conduits for recycling the hydrogen to the mixing device for mixing hydrogen.3. The system of claim 1 , further comprising a feed-effluent exchanger configured to preheat with feed mixture via indirect heat exchange with the reaction effluent.4. The system of claim 1 , wherein the hydrotreater comprises at least two catalyst beds claim 1 , and wherein:a first catalyst bed comprises a catalyst having hydrogenation activity;a second catalyst bed comprises a catalyst having hydrocracking activity.5. The system of claim 1 , wherein the catalyst bed proximate an inlet of the hydrotreater comprises a catalyst useful for at least one of:decarboxylation;{'b': 5 ...

CONVERSION OF TRIACYLGLYCERIDES-CONTAINING OILS

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include reacting a triacylglycerides-containing oil-carbon dioxide mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides to a hydrocarbon or mixture of hydrocarbons comprising one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics. 1. A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels , the process comprising:reacting, in the absence of an added catalyst, a triacylglycerides-containing oil-carbon dioxide mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides to a hydrocarbon or mixture of hydrocarbons comprising one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics.2. The process of claim 1 , further comprising mixing a triacylglycerides-containing oil with carbon dioxide to form the triacylglycerides-containing oil-carbon dioxide mixture.3. The process of claim 1 , further comprising mixing a triacylglycerides-containing oil with carbon dioxide and water to form the triacylglycerides-containing oil-carbon dioxide mixture.4. The process of claim 1 , wherein the triacylglycerides-containing oil-carbon dioxide mixture has a CO2 to triacylglycerides mass ratio in the range from about 0.001:1 to about 1:1.5. The process of claim 1 , further comprising recovering a reaction effluent comprising the reacted triacylglycerides-containing oil-carbon dioxide mixture.6. The process of claim 5 , further comprising separating the reaction effluent to recover a first separation product comprising carbon dioxide and a second separation product comprising the hydrocarbons.7. The ...

CONVERSION OF TRIACYLGLYCERIDES-CONTAINING OILS TO HYDROCARBONS

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include: reacting a triacylglycerides-containing oil-water-hydrogen mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides and recovering a reaction effluent comprising water and one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics; hydrotreating the reaction effluent to form a hydrotreated effluent. 1. A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels , the process comprising:reacting a triacylglycerides-containing oil-water-hydrogen mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides and recovering a reaction effluent comprising water and one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics;hydrotreating the reaction effluent to form a hydrotreated effluent.2. The process of claim 1 , further comprising mixing a triacylglycerides-containing oil with water and hydrogen to form the triacylglycerides-containing oil-water-hydrogen mixture.3. The process of claim 1 , further comprising mixing a triacylglycerides-containing oil with water to form a triacylglyceride-containing oil-water mixture.4. The process of claim 3 , further comprising mixing the triacylglyceride-containing oil-water mixture with hydrogen to form the triacylglycerides-containing oil-water-hydrogen mixture.5. The process of claim 1 , wherein the triacylglycerides-containing oil-water-hydrogen mixture has a water to triacylglycerides mass ratio in the range from about 0.001:1 to about 1:1.6. The process of claim 1 , wherein the triacylglycerides-containing oil-water-hydrogen mixture has a ...

Conversion of asphaltenic pitch within an ebullated bed residuum hydrocracking process

A process for upgrading residuum hydrocarbons including: feeding pitch, hydrogen, and a partially spent catalyst recovered from a hydrocracking reactor to an ebullated bed pitch hydrocracking reactor; contacting the pitch, hydrogen, and the catalyst in the ebullated bed pitch hydrocracking reactor at reaction conditions of temperature and pressure sufficient to convert at least a portion of the pitch to distillate hydrocarbons; and separating the distillate hydrocarbons from the catalyst. In some embodiments, the process may include selecting the ebullated bed pitch hydrocracking reactor reaction conditions to be at or below the level where sediment formation would otherwise become excessive and prevent continuity of operations.

SYSTEM FOR UPGRADING RESIDUUM HYDROCARBONS

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system. 1. A system for upgrading residuum hydrocarbons , the system comprising:a first ebullated bed hydroconversion reactor system for contacting a residuum hydrocarbon fraction and hydrogen to produce a first effluent;a second ebullated bed hydroconversion reactor system for contacting a deasphalted oil fraction and hydrogen to produce a second effluent; anda first fractionation unit to fractionate the first effluent and the second effluent to recover one or more hydrocarbon fractions comprising a vacuum residuum fraction;a solvent deasphalting unit to solvent deasphalt the vacuum residuum fraction to produce the deasphalted oil fraction and an asphalt fraction;a third ebullated bed hydroconversion reactor system for contacting the asphalt fraction and hydrogen to produce a third effluent; anda second fractionation unit to fractionate the third effluent to recover one or more hydrocarbon fractions.2. The system of claim 1 , wherein the fractionation unit is fluidly coupled to at least one of the solvent deasphalting unit claim 1 , a vacuum distillation system ...

Method for making middle distillates and a heavy vacuum gas oil fcc feedstock

The present invention is directed to a refining process for producing hydroprocessed distillates and a heavy vacuum gas oil (HVGO). The process produces middle distillates that have reduced nitrogen and sulfur content, while simultaneously producing a 900° F. + (482° C. + ) HVGO stream useful as a fluidized catalytic cracking (FCC) unit feedstock.

INTEGRATION OF RESIDUE HYDROCRACKING AND SOLVENT DEASPHALTING

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system. 1. A process for upgrading residuum hydrocarbons , the process comprising:contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system;recovering a first effluent from the first ebullated bed hydroconversion reactor system;solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction;contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system;recovering a second effluent from the second hydroconversion reactor system; andfractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system.2. The process of claim 1 , further comprising:contacting the asphalt fraction and hydrogen with a third hydroconversion catalyst in a third ebullated bed ...

UPGRADING RAW SHALE-DERIVED CRUDE OILS TO HYDROCARBON DISTILLATE FUELS

Integrated processes for upgrading crude shale-derived oils, such as those produced by oil shale retorting or by in situ extraction or combinations thereof. Processes disclosed provide for a split-flow processing scheme to upgrade whole shale oil. The split flow concepts described herein, i.e., naphtha and kerosene hydrotreating in one or more stages and gas oil hydrotreating in one or more stages, requires additional equipment as compared to the alternative approach of whole oil hydrotreating. While contrary to conventional wisdom as requiring more capital equipment to achieve the same final product specifications, the operating efficiency vis a vis on-stream time efficiency and product quality resulting from the split flow concept far exceed in value the somewhat incrementally higher capital expenditure costs. 1. An integrated process for upgrading crude shale-derived oils produced by oil shale retorting or by in situ extraction or by mixtures thereof that includes the following steps:(a) fractionating the whole shale oil into a first fraction comprising naphtha, kerosene and diesel and an atmospheric bottoms fraction comprising gas oil and residuum;(b) contacting the first fraction and hydrogen in a first-stage hydroprocessing reactor containing a hydrogenation catalyst to saturate diolefins contained in the first fraction and recovering an effluent from the first-stage hydroprocessing reactor;(c) feeding the effluent from the first-stage hydroprocessing reactor of step (b) without phase separation to a second-stage hydroprocessing reactor operated in an upflow mode and containing catalysts to perform hydrodemetallization and saturation of mono-olefins in the effluent from the first-stage hydroprocessing reactor and recovering an effluent from the second-stage hydroprocessing reactor;(d) feeding the effluent from the second-stage hydroprocessing reactor of step (c) without phase separation to a third-stage hydroprocessing reactor having one or more beds of ...

RESIDUE HYDROCRACKING PROCESSING

A process for upgrading residuum hydrocarbons and decreasing tendency of the resulting products toward asphaltenic sediment formation in downstream processes is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a hydroconversion catalyst in a hydrocracking reaction zone to convert at least a portion of the residuum hydrocarbon fraction to lighter hydrocarbons; recovering an effluent from the hydrocracking reaction zone; contacting hydrogen and at least a portion of the effluent with a resid hydrotreating catalyst; and separating the effluent to recover two or more hydrocarbon fractions. 1. A process for upgrading residuum hydrocarbons , the process comprising:solvent deasphalting a residuum hydrocarbon fraction to produce a deasphalted oil fraction and an asphalt fraction;contacting the asphalt fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system;recovering an effluent from the first ebullated bed hydroconversion reactor system;fractionating the effluent from the first ebullated bed hydroconversion reactor system to recover one or more hydrocarbon fractions.2. The process of claim 1 , further comprising mixing the asphalt fraction with a diluent to form a diluted asphalt fraction prior to the contacting.3. The process of claim 2 , wherein the diluent comprises at least one of FCC cycle oils claim 2 , slurry oils claim 2 , aromatics extracts claim 2 , and straight run vacuum gas oils.4. The process of claim 1 , further comprising:contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a residue hydrodesulfurization unit;recovering an effluent from the residue hydrodesulfurization unit;contacting the residue hydrodesulfurization unit effluent or a portion thereof with a third hydroconversion catalyst in a hydrocracking reactor system;recovering an effluent from the hydrocracking reactor system;fractionating the effluent ...

PROCESS TO UPGRADE PARTIALLY CONVERTED VACUUM RESIDUA

Processes for upgrading partially converted vacuum residua hydrocarbon feeds are disclosed. The upgrading processes may include: steam stripping the partially converted vacuum residua to generate a first distillate and a first residuum; solvent deasphalting the first residuum stream to generate a deasphalted oil and an asphaltenes fraction; vacuum fractionating the deasphalted oil to recover a deasphalted gas oil distillate and a heavy deasphalted residuum; contacting the first distillate and the deasphalted gas oil distillate and hydrogen in the presence of a first hydroconversion catalyst to produce a product; contacting the heavy deasphalted residuum stream and hydrogen in the presence of a second hydroconversion catalyst to produce an effluent; and fractionating the effluent to recover a hydrocracked atmospheric residua and a hydrocracked atmospheric distillate 1. A process for upgrading a partially converted vacuum residua , comprising:stripping the partially converted vacuum residua utilizing a non-reactive stripping medium to generate a first distillate and a first residuum;solvent deasphalting the first residuum to generate a deasphalted oil and an asphaltenes fraction;vacuum fractionating the deasphalted oil to recover a deasphalted gas oil distillate and a heavy deasphalted residuum;contacting the first distillate and the deasphalted gas oil distillate and hydrogen in the presence of a first hydroprocessing catalyst to produce a first hydroprocessing effluent;contacting the heavy deasphalted residuum and hydrogen in the presence of a second hydroconversion catalyst to produce a second hydroprocessing effluent; andfractionating the second hydroprocessing effluent to recover a hydrocracked atmospheric residua and a hydrocracked atmospheric distillate.2. The process of claim 1 , wherein the partially converted vacuum residua comprises an effluent from an upstream conversion process.3. The process of claim 1 , further comprising solvent deasphalting the ...

CO-CURRENT ADIABATIC REACTION SYSTEM FOR CONVERSION OF TRIACYLGLYCERIDES RICH FEEDSTOCKS

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include: reacting a triacylglycerides-containing oil-water-hydrogen mixture in a single reactor at a temperature in the range from about 250° C. to about 650° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides via homogeneously catalyzed hydrothermolysis and heterogeneously catalyzed hydrotreatment. 1. A process for converting triacylglycerides-containing oils or fatty acids derived from plants , algae , organic wastes or animal sources into crude oil precursors and/or distillate hydrocarbon fuels , the process comprising:feeding hydrogen, water, and a triacylglyceride-containing oil into a co-current reactor having a homogeneously catalyzed hydrothermolysis reaction zone and a heterogeneously catalyzed hydrotreatment zone;hydrothermolyzing at least a portion of the triacylglyceride-containing oil in the hydrothermolysis reaction zone to form a hydrothermolysis reaction product; andhydrotreating the hydrothermolysis reaction product directly without any componential separations in the catalytic hydrotreatment zone; andrecovering an effluent from the catalytic hydrotreatment zone.2. The process of claim 1 , wherein the hydrothermolysis reaction zone and the catalytic hydrotreatment zone are adiabatic reaction zones.3. The process of claim 1 , wherein the hydrothermolysis reaction zone and the catalytic hydrotreatment zone are contained within the same reactor vessel.4. The process of claim 3 , wherein the hydrothermolysis reaction zone contains one or more beds of inert solids to promote mixing.5. The process of claim 3 , wherein the catalytic hydrotreatment zone comprises one or more beds containing one or more hydrotreating catalysts.6. The process of claim 1 , further comprising feeding at least one of hydrogen and water intermediate the hydrothermolysis reaction zone ...

INTEGRATION OF RESIDUE HYDROCRACKING AND HYDROTREATING

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system. 1. A process for upgrading residuum hydrocarbons , the process comprising:contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydro conversion reactor system;recovering a first effluent from the first ebullated bed hydroconversion reactor system;contacting the first effluent and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system;recovering a second effluent from the second hydroconversion reactor system;contacting the second effluent and hydrogen with a third hydroconversion catalyst in a second ebullated bed hydroconversion reactor system;recovering a third effluent from the second ebullated bed hydroconversion reactor system; andfractionating the third effluent from the second ebullated bed hydroconversion reactor system to recover one or more hydrocarbon fractions.2. The process of claim 1 , wherein the second hydroconversion reactor system comprises a fixed bed reactor.3. The process of claim 1 , further comprising recycling a vacuum residuum ...

HYDROPROCESSING THERMALLY CRACKED PRODUCTS

Embodiments herein relate to a process flow scheme for the processing of gas oils and especially reactive gas oils produced by thermal cracking of residua using a split flow concept. The split flow concepts disclosed allow optimization of the hydrocracking reactor seventies and thereby take advantage of the different reactivities of thermally cracked gas oils versus those of virgin gas oils. This results in a lower cost facility for producing base oils as well as diesel, kerosene and gasoline fuels while achieving high conversions and high catalyst lives. 1. A process for upgrading gas oils to distillate hydrocarbons , the process comprising:dividing a first gas oil stream into a first and second portions;mixing a second gas oil stream and the first portion of the first gas oil stream to form a mixed gas oil stream;contacting the mixed gas oil stream and hydrogen with a first hydroconversion catalyst in a first hydrocracker reaction system to convert at least a portion of the hydrocarbons in the mixed gas oil stream to distillate hydrocarbons;recovering an effluent from the first hydrocracker reaction system comprising unconverted hydrocarbons and the distillate hydrocarbons;fractionating the effluent from the first hydrocracker reaction system into one or more hydrocarbon fractions including a fraction comprising the unconverted hydrocarbons;contacting hydrogen and the fraction comprising the unconverted hydrocarbons with a second hydroconversion catalyst in a second hydrocracker reaction system to convert at least a portion of the hydrocarbons in the mixed gas oil stream to distillate hydrocarbons;feeding the effluent from the second hydrocracking reaction system to the fractionating step for concurrent fractionation with the effluent from the first hydrocracker reaction system;contacting hydrogen and the second portion of the first gas oil stream with a third hydroconversion catalyst in a third hydrocracker reaction system to convert at least a portion of the ...

MULTI-STAGE RESID HYDROCRACKING

Processes and systems for upgrading resid hydrocarbon feeds are disclosed. The process system may operate in two different operating modes, maximum conversion and maximum quality effluent. The process system may be reversibly transitioned between the different operating modes. The system has the ability to reversibly transition between the two modes without shutting down the system or losing production. 1. A process for upgrading resid , comprising:feeding hydrogen and a resid hydrocarbon to a first ebullated bed reactor containing a first hydrocracking catalyst;contacting the resid and hydrogen in the presence of the hydrocracking catalyst at conditions of temperature and pressure to crack at least a portion of the resid;separating a product from the first reactor into a first gas phase and a first liquid phase product;feeding hydrogen and a deasphalted oil hydrocarbon fraction and a vacuum distillate hydrocarbon fraction to a second ebullated bed reactor containing a hydrotreating catalyst;contacting the deasphalted oil hydrocarbon fraction, the vacuum distillate hydrocarbon fraction and hydrogen in the presence of the hydrotreating catalyst at conditions of temperature and pressure to hydrotreat at least a portion of the deasphalted oil hydrocarbon fraction and the vacuum distillate hydrocarbon fraction;separating a product from the second reactor into a second gas phase and a second liquid phase product;separating the second liquid phase product into a second reactor effluent and a residual fluid catalytic cracking (RFCC) feed;fractionating the first liquid phase product and the second reactor effluent to form at least one distillate hydrocarbon fraction, the vacuum distillate hydrocarbon fraction, and at least one resid hydrocarbon fraction; andfeeding the at least one resid hydrocarbon fraction to a solvent deasphalting unit to provide an asphaltene fraction and the deasphalted oil hydrocarbon fraction.2. The process of claim 1 , wherein the fractionating ...

PROCESS FOR PRODUCING DISTILLATE FUELS AND ANODE GRADE COKE FROM VACUUM RESID

A process for upgrading residuum hydrocarbon feedstocks that may include: contacting a residuum hydrocarbon and hydrogen with a hydroconversion catalyst in a residuum hydroconversion reactor system; recovering an effluent from the residuum hydroconversion reactor system; separating the effluent to recover two or more hydrocarbon fractions including at least a vacuum residuum fraction and a heavy vacuum gas oil fraction; combining at least a portion of the heavy vacuum gas oil fraction and at least a portion of the vacuum residuum fraction to form a mixed heavy hydrocarbon fraction; feeding at least a portion of the mixed heavy hydrocarbon fraction to a coker; operating the coker at conditions to produce anode grade green coke and distillate hydrocarbons; recovering the distillate hydrocarbons from the coker; fractionating the distillate hydrocarbons to recover hydrocarbon fractions including a light distillates fraction, a heavy coker gas oil fraction, and a coker recycle fraction. 1. A process for upgrading residuum hydrocarbon feedstocks , comprising:contacting a residuum hydrocarbon and hydrogen with a hydroconversion catalyst in an residuum hydroconversion reactor system;recovering an effluent from the residuum hydroconversion reactor system;separating the effluent from the residuum hydroconversion reactor system to recover two or more hydrocarbon fractions including at least a vacuum residuum fraction and a heavy vacuum gas oil fraction;combining at least a portion of the heavy vacuum gas oil fraction and at least a portion of the vacuum residuum fraction to form a mixed heavy hydrocarbon fraction;feeding at least a portion of the mixed heavy hydrocarbon fraction to a coker;operating the coker at conditions to produce anode grade green coke and distillate hydrocarbons;recovering the distillate hydrocarbons from the coker;fractionating the distillate hydrocarbons recovered from the coker to recover three or more hydrocarbon fractions including a light ...

Integration of residue hydrocracking and hydrotreating

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system.

CONVERSION OF ALCOHOLS TO DISTILLATE FUELS

A process for the production of jet and other heavy fuels from alcohols and mixture of alcohols is disclosed. The process may include contacting in a reaction zone at least one C2 to C11 alcohol with a solid catalyst having activity for the simultaneous dehydration of the alcohols to form olefins, isomerization of the olefins to form internal olefins, and oligomerization of the olefins produced in situ via the dehydration reaction to form an effluent comprising mono-olefinic hydrocarbons. Preferably, the alcohol feed is a mixture of alcohols, such as C2 to C7 alcohols or C4 and C6 alcohols, enabling the production of a mixture of branched hydrocarbons that may be used directly as a jet fuel without blending. 1. A process for the production of distillate fuels , the process comprising: i. dehydration of the C4 alcohol to form water and C4 olefins,', 'ii. oligomerization of the olefins produced in situ,', 'iii. positional isomerization of the C4 olefins, C8-C12 olefins, and olefin oligomers to form internal olefins, and', 'iv. reaction of the C8-C12 olefins with the olefins produced in situ,', 'to form an effluent comprising branched mono-olefinic distillate fuel range hydrocarbon oligomers;, 'contacting, in a reaction zone, a light olefin feedstock, comprising one or more C8-C12 olefins, and an alcohol feedstock, comprising a C4 alcohol selected from the group consisting of 2-butanol, 1-butanol, and isobutanol or mixtures thereof, with a solid acid catalyst at conditions of temperature and pressure where the solid acid catalyst has activity for the simultaneousseparating the branched mono-olefinic distillate fuel range hydrocarbon oligomers from water and any unreacted alcohol;fractionating the branched mono-olefinic distillate fuel range hydrocarbon oligomers to recover the light olefin feedstock and a heavy oligomer fraction.2. The process of claim 1 , wherein the light olefin feedstock comprises C8 and lighter olefins.3. The process of claim 1 , wherein the light ...

CONVERSION OF ASPHALTENIC PITCH WITHIN AN EBULLATED BED RESIDUUM HYDROCRACKING PROCESS

A process for upgrading residuum hydrocarbons including: feeding pitch, hydrogen, and a partially spent catalyst recovered from a hydrocracking reactor to an ebullated bed pitch hydrocracking reactor; contacting the pitch, hydrogen, and the catalyst in the ebullated bed pitch hydrocracking reactor at reaction conditions of temperature and pressure sufficient to convert at least a portion of the pitch to distillate hydrocarbons; and separating the distillate hydrocarbons from the catalyst. In some embodiments, the process may include selecting the ebullated bed pitch hydrocracking reactor reaction conditions to be at or below the level where sediment formation would otherwise become excessive and prevent continuity of operations. 134.-. (canceled)35. A system for upgrading residuum hydrocarbons , the system comprising:a residuum hydrocarbon conversion reactor system for contacting a residuum hydrocarbon, hydrogen, and a hydrocracking catalyst to convert at least a portion of the residuum hydrocarbon to distillate range hydrocarbons;a separation system for fractionating the distillate range hydrocarbons into two or more hydrocarbon fractions including a vacuum tower bottoms fraction;a separation system for recovering at least some of the spent catalyst from the residuum hydrocarbon conversion reactor system;a grinder for grinding the recovered spent catalyst;a solvent deasphalting unit for solvent deasphalting the vacuum tower bottoms fraction to produce a deasphalted oil fraction and a pitch fraction;a pitch hydrocracking reactor system for contacting the pitch, hydrogen, and the ground spent catalyst at reaction conditions of temperature and pressure sufficient to convert at least a portion of the pitch to distillate hydrocarbons.36. The system of claim 35 , further comprising a separation system for separating the distillate hydrocarbons from the ground spent catalyst.37. The system of claim 35 , wherein the residuum hydrocarbon conversion reactor system comprises ...

CONVERSION OF TRIACYLGLYCERIDES-CONTAINING OILS

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include reacting a triacylglycerides-containing oil-carbon dioxide mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides to a hydrocarbon or mixture of hydrocarbons comprising one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics. 132-. (canceled)33. A system for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels , the system comprising:a mixing device for mixing a triacylglycerides-containing oil feed with carbon dioxide to form an oil-CO2 mixture;a thermal reforming reactor for reacting the oil-CO2 mixture at a temperature in the range of 250° C. to about 525° C. and a pressure greater than about 75 bar to produce a reaction effluent; anda separator for separating the reaction effluent into a first separation product comprising carbon dioxide and a second separation product comprising hydrocarbon compounds including one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics.34. The system of claim 33 , further comprising one or more fluid conduits for recycling the first separation product to at least one of the mixing device to form the oil-CO2 mixture and the thermal reforming reactor to control temperature within the thermal reforming reactor.35. The system of claim 33 , further comprising a hydrotreater to hydrotreat at least a portion of the second separation product.36. The system of claim 33 , further comprising a fractionator for fractionating hydrocarbons in the second separation product to form one or more hydrocarbon fractions boiling in the naphtha claim 33 , jet or diesel range.37. The system of claim 35 , further comprising a fractionator for fractionating hydrocarbons in the ...

PROCESSING VACUUM RESIDUUM AND VACUUM GAS OIL IN EBULLATED BED REACTOR SYSTEMS

A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone. 1. A process for upgrading residuum hydrocarbons and heavy distillate feedstocks , the process comprising:contacting residuum hydrocarbons and hydrogen with a non-zeolitic base metal hydroconversion catalyst in a first ebullated bed hydroconversion reactor system to produce a first effluent;fractionating the first effluent from the first ebullated bed hydroconversion reactor to recover a liquid product and vapor product;contacting the vapor product and a heavy distillate feedstock with a zeolitic selective hydrocracking catalyst in a second ebullated bed hydrocracking reactor system to produce a second effluent;recovering the second effluent from the second ebullated bed hydrocracking reactor system; andfractionating the second effluent from the second ebullated bed hydrocracking reactor system to recover one or more hydrocarbon fractions.2. The process of claim 1 , further comprising heating the residuum hydrocarbons and hydrogen prior to contact with the catalyst.3. The process of claim 1 , wherein the residuum hydrocarbons are selected from one or more of petroleum crudes claim 1 , shale oils claim 1 , tar sands bitumen claim 1 , coal-derived oils claim 1 , tall oils claim 1 , black oils claim 1 , organic wastes claim 1 , biomass-derived liquids or any heavy oil ...

PROCESSING VACUUM RESIDUUM AND VACUUM GAS OIL IN EBULLATED BED REACTOR SYSTEMS

A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone. 1. A system for upgrading residuum hydrocarbons and heavy distillate feedstocks , the system comprising:an ebullated bed hydroconversion reactor system configured to contact residuum hydrocarbons and hydrogen with a non-zeolitic base metal hydroconversion catalyst to produce a first effluent,a first separation unit configured to separate the first effluent to recover a first liquid product and a first vapor product;an absorption tower configured to contact counter-currently the first vapor product with a hydrocarbon stream to produce a second vapor product and a second liquid product, wherein the second vapor product is lean in middle distillate content and comprises gasoil range hydrocarbon;a second separation unit configured to separate the second vapor product from the second liquid product;an ebullated bed hydrocracking reactor system configured to contact the second vapor product and a heavy distillate feedstock with a zeolitic selective hydrocracking catalyst to produce a second effluent, anda third separation unit configured to separate the second effluent and recover one or more hydrocarbon fractions.2. The system of claim 1 , further comprising a heat exchange unit configured to heat the residuum hydrocarbons and hydrogen prior to contact with the non- ...

UPGRADING RAW SHALE-DERIVED CRUDE OILS TO HYDROCARBON DISTILLATE FUELS

Integrated processes for upgrading crude shale-derived oils, such as those produced by oil shale retorting or by in situ extraction or combinations thereof. Processes disclosed provide for a split-flow processing scheme to upgrade whole shale oil. The split flow concepts described herein, i.e., naphtha and kerosene hydrotreating in one or more stages and gas oil hydrotreating in one or more stages, requires additional equipment as compared to the alternative approach of whole oil hydrotreating. While contrary to conventional wisdom as requiring more capital equipment to achieve the same final product specifications, the operating efficiency vis a vis on-stream time efficiency and product quality resulting from the split flow concept far exceed in value the somewhat incrementally higher capital expenditure costs. 126.-. (canceled)27. An integrated system for upgrading crude shale-derived oils produced by oil shale retorting or by in situ extraction or by mixtures thereof that includes the following:a. a fractionator for fractionating the whole shale oil into a first fraction comprising naphtha, kerosene and diesel and an atmospheric bottoms fraction comprising gas oil and residuum;b. a first-stage hydroprocessing reactor containing a hydrogenation catalyst to saturate diolefins contained in the first fraction with hydrogen and having an outlet for recovering an effluent;c. a second-stage hydroprocessing reactor configured to be operated in an upflow mode and containing catalysts to perform hydrodemetallization and saturation of mono-olefins in the effluent from the first-stage hydroprocessing reactor and having an outlet for recovering a second-stage hydroprocessing reactor effluent, wherein the first-stage hydroprocessing reactor and the second-stage hydroprocessing reactor are fluidly connected such that the effluent from the first-stage hydroprocessing reactor is fed to the second-stage hydroprocessing reactor without phase separation;d. a third-stage ...

CONVERSION OF TRIACYLGLYCERIDES-CONTAINING OILS TO JET FUEL RANGE HYDROCARBONS

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include: reacting a triacylglycerides-containing oil-water-diatomic hydrogen mixture at a temperature in the range from about 250° C. to about 560° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides and recovering a reaction effluent comprising water and one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics; and hydrotreating the reaction effluent to form a hydrotreated effluent.

PROCESS TO UPGRADE PARTIALLY CONVERTED VACUUM RESIDUA

Processes for upgrading partially converted vacuum residua hydrocarbon feeds are disclosed. The upgrading processes may include: steam stripping the partially converted vacuum residua to generate a first distillate and a first residuum; solvent deasphalting the first residuum stream to generate a deasphalted oil and an asphaltenes fraction; vacuum fractionating the deasphalted oil to recover a deasphalted gas oil distillate and a heavy deasphalted residuum; contacting the first distillate and the deasphalted gas oil distillate and hydrogen in the presence of a first hydroconversion catalyst to produce a product; contacting the heavy deasphalted residuum stream and hydrogen in the presence of a second hydroconversion catalyst to produce an effluent; and fractionating the effluent to recover a hydrocracked atmospheric residua and a hydrocracked atmospheric distillate. 1. A process for upgrading a partially converted vacuum residua , comprising:stripping the partially converted vacuum residua utilizing a non-reactive stripping medium to generate a first distillate and a first residuum;solvent deasphalting the first residuum to generate a deasphalted oil and an asphaltenes fraction;vacuum fractionating the deasphalted oil to recover a deasphalted gas oil distillate and a heavy deasphalted residuum;contacting the first distillate and the deasphalted gas oil distillate and hydrogen in the presence of a first hydroprocessing catalyst to produce a first hydroprocessing effluent;contacting the heavy deasphalted residuum and hydrogen in the presence of a second hydroconversion catalyst to produce a second hydroprocessing effluent; andseparating the second hydroprocessing effluent to recover a hydrocracked vapor and a hydrocracked liquid.2. The process of claim 1 , wherein the partially converted vacuum residua comprises an effluent from an upstream conversion process.3. The process of claim 1 , further comprising solvent deasphalting the hydrocracked liquid with the first ...

Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization

A process for the double-bond isomerization of olefins is disclosed. The process may include contacting a fluid stream comprising olefins with a fixed bed comprising an activated basic metal oxide isomerization catalyst to convert at least a portion of the olefin to its isomer. The isomerization catalysts disclosed herein may have a reduced cycle to cycle deactivation as compared to conventional catalysts, thus maintaining higher activity over the complete catalyst life cycle.

Catalyst and process for the metathesis of ethylene and butene to produce propylene

A process for producing propylene from a C4 feed containing 2-butene includes contacting said feed with ethylene in a metathesis reaction zone containing a metathesis catalyst under metathesis reaction conditions to provide an effluent including propylene, said metathesis catalyst consisting essentially of a transition metal or oxide thereof supported on a high purity silica support possessing less than about 150 ppm magnesium, less than about 900 ppm calcium, less than about 900 ppm sodium, less than about 200 ppm aluminum, and less than about 40 ppm iron.

Catalyst for the metathesis of olefin(s)

An olefin metathesis catalyst consists essentially of a transition metal or oxide thereof supported on a high purity silica support possessing low amounts of acidic or basic sites such that in the reaction of pure butene-1 over said catalyst under metathesis reaction conditions the reaction possesses a weight selectivity to hexene-3 of at least 55 wt %.

Upgrading raw shale-derived crude oils to hydrocarbon distillate fuels

Integrated processes for upgrading crude shale-derived oils, such as those produced by oil shale retorting or by in situ extraction or combinations thereof. Processes disclosed provide for a split-flow processing scheme to upgrade whole shale oil. The split flow concepts described herein, i.e., naphtha and kerosene hydrotreating in one or more stages and gas oil hydrotreating in one or more stages, requires additional equipment as compared to the alternative approach of whole oil hydrotreating. While contrary to conventional wisdom as requiring more capital equipment to achieve the same final product specifications, the operating efficiency vis a vis on-stream time efficiency and product quality resulting from the split flow concept far exceed in value the somewhat incrementally higher capital expenditure costs.

Processing vacuum residuum and vacuum gas oil in ebullated bed reactor systems

A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone.

Integration of residue hydrocracking and hydrotreating

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebuUated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system.

Conversion of asphaltenic pitch within an ebullated bed residuum hydrocracking process

A process for upgrading residuum hydrocarbons including: feeding pitch, hydrogen, and a partially spent catalyst recovered from a hydrocracking reactor to an ebullated bed pitch hydrocracking reactor; contacting the pitch, hydrogen, and the catalyst in the ebullated bed pitch hydrocracking reactor at reaction conditions of temperature and pressure sufficient to convert at least a portion of the pitch to distillate hydrocarbons; and separating the distillate hydrocarbons from the catalyst. In some embodiments, the process may include selecting the ebullated bed pitch hydrocracking reactor reaction conditions to be at or below the level where sediment formation would otherwise become excessive and prevent continuity of operations.

Integration of residue hydrocracking and hydrotreating

Conversion of triacylglycerides-containing oils to hydrocarbons

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include: reacting a triacylglycerides-containing oil-water-hydrogen mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides and recovering a reaction effluent comprising water and one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics; hydrotreating the reaction effluent to form a hydrotreated effluent.

Multistage resid hydrocracking

Processes and systems for upgrading resid hydrocarbon feeds are disclosed. The process system may operate in two different operating modes, maximum conversion and maximum quality effluent. The process system may be reversibly transitioned between the different operating modes. The system has the ability to reversibly transition between the two modes without shutting down the system or losing production.

Olefin isomerization process

An olefin isomerization process employs a basic metal oxide catalyst, such as magnesium oxide. The catalyst is preferably a high purity magnesium oxide. The olefin isomerization process and catalyst described herein are advantageously used for the production of a terminal olefin such as 1-butene from an internal olefin such as 2-butene.

Olefin isomerization process

An olefin isomerization process employs a basic metal oxide catalyst, such as magnesium oxide, which retains at least about 85 percent of its initial activity for at least about 168 hours of on-stream time. The catalyst is preferably a high purity magnesium oxide. The olefin isomerization process and catalyst described herein are advantageously used for the production of a terminal olefin such as 1-butene from an internal olefin such as 2-butene.

System and process for producing linear alpha olefins

Processes and systems for producing linear alpha olefins are described herein. One embodiment is a process comprising: a) separating a mixed butene stream comprising 1-butene and 2-butene into an overhead 1-butene stream and a bottoms 2-butene stream in a butene distillation column, a portion of the bottoms 2-butene stream being separated to form a butene reboil-er stream that is heated and vaporized in a reboiler and returned to the butene distillation column, (b) subjecting at least a portion of the overhead 1-butene stream from (a) to catalytic metathesis to produce an effluent including 3-hexene, (c) isomerizing 3-hexene from (b) to produce a mixed hexene stream comprising 1-hexene, 2-hexene and 3-hexene, (d) separating the mixed hexene stream in a hexene fractionation tower to form a 1-hexene vapor overhead stream that is condensed in a cooler and a bottoms stream comprising 2-hexene and 3-hexene, and (e) using heat obtained by condensing the 1-hexene vapor overhead stream of (d) to heat the butene reboiler stream of (a). Another embodiment is a superfractionation process. Corresponding systems are also disclosed.

Conversion of triacylglycerides-containing oils to jet fuel range hydrocarbons

Olefin isomerization process

An olefin isomerization process employs a basic metal oxide catalyst, such a s magnesium oxide. The catalyst is preferably a high purity magnesium oxide. T he olefin isomerization process and catalyst described herein are advantageousl y used for the production of a terminal olefin such as 1-butene from an intern al olefin such as 2-butene.

Integration of residue hydrocracking and hydrotreating

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebuUated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system.

Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization

Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization

A process for the double-bond isomerization of olefins is disclosed. The process may include contacting a fluid stream comprising olefins with a fixed bed comprising an activated basic metal oxide isomerization catalyst to convert at least a portion of the olefin to its isomer. The isomerization catalysts disclosed herein may have a reduced cycle to cycle deactivation as compared to conventional catalysts, thus maintaining higher activity over the complete catalyst life cycle.

Processing c4 olefin streams for the maximum production of propylene

In order to maximize the production of propylene when the external supply of ethylene is limited, the C4 cut from a hydrocarbon cracking process is first subjected to autometathesis prior to any isobutylene removal and without any ethylene addition. This favors the reactions which produce propylene and pentenes. The ethylene and propylene produced are then removed leaving a stream of the C4~s and heavier components. The C5 and heavier components are then removed leaving a mixture of 1-butene, 2-butene, isobutylene, and iso-and normal butanes. The isobutylene is next removed preferably by a catalytic distillation hydroisomerization de-isobutyleneizer. The isobutylene-free C4 stream is then mixed with the product ethylene removed from the autometathesis product together with any fresh external ethylene needed and subjected to conventional metathesis producing additional propylene.

Conversion of triacylglycerides-containing oils

Processing vacuum residuum and vacuum gas oil in ebullated bed reactor systems

Processing c 4- olefin streams for the maximum production of propylene

In order to maximize the production of propylene when the external supply of ethylene is limited, the C4 cut from a hydrocarbon cracking process is first subjected to autometathesis prior to any isobutylene removal and without any ethylene addition. This favors the reactions which produce propylene and pentenes. The ethylene and propylene produced are then removed leaving a stream of the C4’s and heavier components. The C5 and heavier components are then removed leaving a mixture of 1-butene, 2-butene, isobutylene, and iso-and normal butanes. The isobutylene is next removed preferably by a catalytic distillation hydroisomerization de-isobutyleneizer. The isobutylene-free C4 stream is then mixed with the product ethylene removed from the autometathesis product together with any fresh external ethylene needed and subjected to conventional metathesis producing additional propylene.

butane removal in c4 level up processes

REMOçãO DE BUTANO EM PROCESSOS DE AUMENTO DE NìVEL DE C4. A presente invenção refere-se a um processo para produção de um butano selecionado, que compreende obter um fluxo de alimentação 04 que por sua vez compreende parafinas 04 e olefinas 04, dividir o fluxo de alimentação 04 com a finalidade de formar um primeiro fluxo que compreen- de um primeiro butano e um segundo fluxo que compreende um segundo butano, isomerizar ao menos parte do segundo fluxo de modo a converter uma porção do segundo butano em primeiro butano, e reciclar ao menos alguma parte isomerizada de um segundo fluxo em relação à etapa de divisão, onde uma porção de ao menos um fluxo de alimentação 04 e segundo fluxo passa através de uma membrana de transporte facilitado com a finalidade de remover butanos, formando ao menos um fluxo de purificação que compreende butanos. Trata-se, também, de um processo para conversão de olefinas 04, que compreende obter um fluxo de alimentação 04 que por sua vez compreende parafinas 04 e olefinas 04, incluindo 1-butano e 2-buteno, e reagir o fluxo de alimentação 04 em um reator de metátese de modo a formar um segundo fluxo. O segundo fluxo é fracionado com a finalidade de formar um ou mais fluxos de produção e um fluxo de reciclagem que contém, primariamente, olefinas 04 e parafinas 04. O fluxo de reciclagem e/ou o fluxo de alimentação 04 passam através de uma membrana de transporte facilitado para remover, formando ao menos um fluxo de purificação. BUTANE REMOVAL IN C4 LEVEL INCREASE PROCESSES. The present invention relates to a process for the production of a selected butane, which comprises obtaining a feed stream 04 which in turn comprises paraffins 04 and olefins 04, dividing the feed stream 04 in order to form a first stream which comprising a first butane and a second stream comprising a second butane, isomerizing at least part of the second stream in order to convert a portion of the second butane to first butane, and recycling at least some isomerized part ...

Process and apparatus for producing distillate fuels and anode grade coke from vacuum resid

Processing vacuum residuum and vacuum gas oil in ebullated bed reactor systems

Cyclohexane oxidation

Cyclohexane is catalytically oxidized to produce cyclohexanol and cyclohexanone and precursors of these products. The product is then catalytically hydrogenated while the product is still at reaction temperature to produce additional cyclohexanol and cyclohexanone from the precursors. The oxidation is carried out in a liquid oxidation reactor at high oxygen concentrations (greater than 30% and preferably greater than 90% oxygen concentration) and at relatively low temperatures (less than 160° C.). The use of the liquid oxidation reactor permits the use of these high oxygen concentrations without forming dangerously high levels of oxygen in the overhead gas phase. The result is an increased yield and selectivity of the desired products. The hydrogenation is carried out in a reactor using a catalyst of palladium supported on carbon.

Process and system to upgrade partially converted vacuum residua

Catalyst consisting of a transition metal supported on a high purity silica for the metathesis of olefin(s)

An olefin metathesis catalyst consists essentially of a transition metal or oxide thereof, preferably tungsten oxide, supported on a high purity silica support possessing less than 150 ppm Mg, less than 900 ppm Ca, less than 900 ppm Na, less than 200 ppm Al, and less than 40 ppm Fe. The support possesses low amounts of acidic or basic sites such that in the reaction of pure butene-1 over said catalyst under metathesis reaction conditions the reaction possesses a weight selectivity to hexene-3 of at least 55 wt%.

Conversion of triacylglycerides-containing oils to jet fuel range hydrocarbons

Process for producing distillate fuels and anode grade coke from vacuum resid

CRACKING PROCESS WITH HYDROGEN DONOR SOLVENT AND PROCESS FOR PROCESSING CRUDE OIL

Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization

A process for the double-bond isomerization of olefins is disclosed. The process may include contacting a fluid stream comprising olefins with a fixed bed comprising an activated basic metal oxide isomerization catalyst to convert at least a portion of the olefin to its isomer. The isomerization catalysts disclosed herein may have a reduced cycle to cycle deactivation as compared to conventional catalysts, thus maintaining higher activity over the complete catalyst life cycle.

Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization

System and process for producing linear alpha olefins

Processes and systems for producing linear alpha olefins are described herein. One embodiment is a process comprising: a) separating a mixed butene stream comprising 1 -butene and 2-butene into an overhead 1 -butene stream and a bottoms 2-butene stream in a butene distillation column, a portion of the bottoms 2-butene stream being separated to form a butene reboiler stream that is heated and vaporized in a reboiler and returned to the butene distillation column, (b) subjecting at least a portion of the overhead 1 -butene stream from (a) to catalytic metathesis to produce an effluent including 3-hexene, (c) isomerizing 3-hexene from (b) to produce a mixed hexene stream comprising 1 -hexene, 2-hexene and 3-hexene, (d) separating the mixed hexene stream in a hexene fractionation tower to form a 1 -hexene vapor overhead stream that is condensed in a cooler and a bottoms stream comprising 2-hexene and 3-hexene, and (e) using heat obtained by condensing the 1 -hexene vapor overhead stream of (d) to heat the butene reboiler stream of (a). Another embodiment is a superfractionation process. Corresponding systems are also disclosed.

Method for making middle distillates and a heavy vacuum gas oil fcc feedstock

The present invention is directed to a refining process for producing hydroprocessed distillates and a heavy vacuum gas oil (HVGO). The process produces middle distillates that have reduced nitrogen and sulfur content, while simultaneously producing a 900°F+ (482°C+) HVGO stream useful as a fluidized catalytic cracking (FCC) unit feedstock.

Conversion of triacylglycerides-containing oils

揭露一種用於將含三酸甘油酯之油轉化為粗製油先質及/或餾出物烴燃料之方法。此方法可包含將一含三酸甘油酯之油-二氧化碳之混合物於範圍從約250℃至約560℃之溫度及大於約75巴之壓力反應，以將至少一部份之三酸甘油酯轉化為包含異烯烴、異烷烴、環烯烴、環烷烴，及芳香族化合物之一或多種的烴或烴混合物。於某些實施例，將三酸甘油酯轉化為烴產物可有利地於無添加水及添加氫實施。

Butane removal in c4 upgrading processes

Disclosed herein is a process for producing a selected butane, comprising obtaining a C4 feed stream comprising C4 paraffins and C4 olefins, splitting the C4 feed stream to form a first stream comprising a first butane and a second stream comprising a second butane, isomerizing at least a part of the second stream to convert a portion of the second butane to the first butane, and recycling at least some of the isomerized part of the second steam to the splitting step, wherein a portion of at least one of the C4 feed stream and the second stream is passed through a facilitated transport membrane to remove butanes, forming at least one purge stream comprising butanes. A process for the conversion of C4 olefins, comprising obtaining a C4 feed stream comprising C4 paraffins and C4 olefins, including 1 -butane and 2-butene, and reacting the C4 feed stream in a metathesis reactor to form a second stream is also disclosed. The second stream is fractionated to form one or more product streams and a recycle stream primarily containing C4 olefins and C4 paraffins. The recycle stream and/or the C4 feed stream is passed through a facilitated transport membrane to remove butanes, forming at least one purge stream.

Processing vacuum residuum and vacuum gas oil in ebullated bed reactor systems

A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone.

Processing vacuum residuum and vacuum gas oil in ebullated bed reactor systems

A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone.

Conversion of triacylglyceride-containing oils to hydrocarbons

Catalyst consisting of a transition metal supported on a high purity silica for the metathesis of olefin(s)

An olefin metathesis catalyst consists essentially of a transition metal or oxide thereof, preferably tungsten oxide, supported on a high purity silica support possessing less than 150 ppm Mg, less than 900 ppm Ca, less than 900 ppm Na, less than 200 ppm Al, and less than 40 ppm Fe. The support possesses low amounts of acidic or basic sites such that in the reaction of pure buten e- 1 over said catalyst under metathesis reaction conditions the reaction possesses a weight selectivity to hexene-3 of at least 55 wt%.

Patent DE3207069C2

Residue hydrocracking processing.

Se describe un proceso para mejorar hidrocarburos de residuos indestilables del crudo y disminuir la tendencia de los productos resultantes hacia la formación de sedimentos asfalténicos en procesos corriente abajo. El proceso puede incluir: poner en contacto una fracción de hidrocarburo de residuos indestilables del crudo e hidrógeno con un catalizador de hidroconversión en una zona de reacción de hidrocraqueo para convertir al menos una porción de la fracción de hidrocarburos de residuos indestilables del crudo a hidrocarburos más ligeros; recuperar un efluente de la zona de reacción de hidrocraqueo; poner en contacto el hidrógeno y al menos una porción del efluente con un catalizador de hidrotratamiento de residuos; y separar el efluente para recuperar dos o más fracciones de hidrocarburo.

System and process for conversion of triacylglycerides-containing oils to hydrocarbons

Residue hydrocracking processing

A process for upgrading residuum hydrocarbons and decreasing tendency of the resulting products toward asphaltenic sediment formation in downstream processes is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a hydroconversion catalyst in a hydrocracking reaction zone to convert at least a portion of the residuum hydrocarbon fraction to lighter hydrocarbons; recovering an effluent from the hydrocracking reaction zone; contacting hydrogen and at least a portion of the effluent with a resid hydrotreating catalyst; and separating the effluent to recover two or more hydrocarbon fractions.

Process to upgrade partially converted vacuum residua

Processes for upgrading partially converted vacuum residua hydrocarbon feeds are disclosed. The upgrading processes may include: steam stripping the partially converted vacuum residua (10) to generate a first distillate (15) and a first residuum (16); solvent deasphalting the first residuum (16) stream to generate a deasphalted oil (18) and an asphaltenes fraction (20); vacuum fractionating the deasphalted oil (18) to recover a deasphalted gas oil distillate (26) and a heavy deasphalted residuum (30); contacting the first distillate (15) and the deasphalted gas oil distillate (26) and hydrogen (13) in the presence of a first hydroconversion catalyst to produce a product; contacting the heavy deasphalted residuum stream (30) and hydrogen in the presence of a second hydroconversion catalyst to produce an effluent (24); and fractionating the effluent (24) to recover a hydrocracked atmospheric residua (95) and a hydrocracked atmospheric distillate (42).

Processo para aprimorar resíduo a vácuo e sistema para aprimorar hidrocarbonetos residuais

processo para aprimorar resíduo a vácuo e sistema para aprimorar hidrocarbonetos residuais. o presente documento revela processos para aprimorar alimentações de resíduos parcialmente convertidos a vácuo. o processo de aprimoramento pode incluir: remoção a vapor dos resíduos parcialmente convertidos a vácuo para gerar um primeiro destilado e um primeiro resíduo; desasfaltação com solvente da primeira corrente residual para gerar um óleo desasfaltado e uma fração de asfaltenos; fracionamento a vácuo do óleo desasfaltado para recuperar um destilado de gasóleo desasfaltado e um resíduo desasfaltado pesado; contato do primeiro destilado e o destilado de gasóleo desasfaltado e hidrogênio na presença de um primeiro catalisador de hidroconversão para produzir um produto; contato da corrente de resíduo desasfaltado pesado e hidrogênio na presença de um segundo catalisador de hidroconversão para produzir um segundo efluente; e fracionamento do efluente para recuperar um resíduo atmosférico hidrocraqueado e um destilado atmosférico hidrocraqueado.

Co-current adiabatic reaction system for conversion of triacylglycerides rich feedstocks

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include: reacting a triacylglycerides-containing oil-water-hydrogen mixture in a single reactor at a temperature in the range from about 250°C to about 650°C and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides via homogeneously catalyzed hydrothermolysis and heterogeneously catalyzed hydrotreatment.

System and process for producing linear alpha olefins

sistema de reação adiabática co-corrente para conversão de matérias-primas ricas em triacilglicerídeos.

Multistage resid hydrocracking

Processes and systems for upgrading resid hydrocarbon feeds are disclosed. The process system may operate in two different operating modes, maximum conversion and maximum quality effluent. The process system may be reversibly transitioned between the different operating modes. The system has the ability to reversibly transition between the two modes without shutting down the system or losing production. Figure 1

Processing vacuum residuum and vacuum gas oil in ebullated bed reactor systems

A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone. (Figure 1)