Uop Lcc

Other

Eni S.p.a.

John Anthony Petri

Peter Kokayeff

Terry L Marker

Vedula Kasipati Murty

Vasant P Thakkar

Robert C Mulvaney, Iii

Massimo Sangalli

Jacques J L Romatier

Yoga R Ayar

Gregory J Gajda

Bryan K Glover

Charles P Luebke

Antoine Negiz

Andrea G Bozzano

Suheil F Abdo

Hayim Abrevaya

Lisa M Knight

Richard R Willis

Mary Jo Wier

Ping Sun

Kiran Ladkat

Geoffrey William Fichtl

Franco Baldiraghi

Giovanni Faraci

Sailesh B Kumar

Andrew J Towarnicky

Shurong Yang

Jan De Ren

Luigina Maria Flora Sabatino

Silvia Guanziroli

Joseph T Kozlowski

Dhineshkumar Kandaraj

Kenneth J Stippich, Jr

Magaly Estremera

Ashwin Singh Tensingh

Pallavi Luharuka

Terry Louise Marker

Luigina Maria Sabatino

A process for hydroprocessing a sustainable feedstock is disclosed. The process comprises hydrocracking a hydrocracking feed stream comprising greater than 90% paraffins in a hydrocracking reactor in the presence of hydrogen over a hydrocracking catalyst comprising one or more Group VIII metal and/or Group VIB to provide a hydrocracked stream. The hydrocracking reactor is operated at a temperature of about 290° C. (550° F.) to about 450° C. (842° F.) and a pressure of about 2.7 MPa (gauge) (400 psig) to about 20.7 MPa (gauge) (3000 psig). The hydrocracked stream is hydroisomerized in a hydroisomerization reactor in the presence of hydrogen over a hydroisomerization catalyst to provide a hydroisomerized stream. The hydroisomerized stream is separated to provide a jet fuel stream, a diesel stream, and an unconverted oil stream.

Process and apparatus for hydroprocessing a paraffinic feedstock

The process and apparatus of the disclosure utilize a heater between a hydroprocessing reactor and a hydroisomerization reactor. A hydroprocessing feed exchanger cools hydroprocessed effluent to effect turndown of heated hydroprocessed effluent so as to not feed the hydroprocessed effluent to the hydroisomerization reactor at a higher temperature than necessary.

Apparatus and process for heating hydroisomerization feed

A hydrocracking process is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream having a T90 temperature of about 204&#xb0; C. (399&#xb0; F.) to about 238&#xb0; C. (460&#xb0; F.), a diesel stream having a T90 temperature of about 360&#xb0; C. (680&#xb0; F.) to about 383&#xb0; C. (721&#xb0; F.) and an unconverted oil stream. The kerosene stream, the unconverted oil stream, and a portion of the diesel stream is recycled to the hydrocracking reactor for hydrocracking.

Process for hydrocracking a hydrocarbon feed stream

Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight, suitably at least about 2.2 and preferably at least about 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%.

Process for producing a naphtha stream

Slurry hydrocracking processes are described. The methods include hydrotreating a heavy residual hydrocarbon feed in a hydrotreating zone under residual hydrotreating conditions to form a hydrotreated effluent. The hydrotreated effluent is separated in an first separator to form an overhead vapor stream and a bottoms stream. The bottoms stream is hydrocracked in a slurry hydrocracking zone under slurry hydrocracking conditions. The effluent from the slurry hydrocracking zone is fractionated in a fractionation zone into at least two streams. Slurry hydrocracking apparatus is also described.

Integrated hydrotreating and slurry hydrocracking process

A catalyst composition comprising a support comprising a mixture of amorphous silica-alumina and non-zeolitic alumina comprising no more than 75 wt % amorphous silica-alumina and having a ratio of moles of silicon to moles of aluminum in the range of about 0.05 to about 0.50. A first hydrogenation metal comprising platinum, a second hydrogenation metal from Group VIIB or Group VIII of the Periodic Table other than platinum and an optional third metal from Group IA of the Periodic Table may be deposited on the support. The ratio of moles of silicon to the moles of the first hydrogenation metal, the second hydrogenation metal and the optional third metal on the support may be between about 15 and about 75.

Composition for opening polycyclic rings in hydrocracking

A process and apparatus for quenching a hydrocracked stream to prepare it for hydroisomerization. A fractionated hydroisomerized stream is recycled to quench a hot hydrocracked stream prior to hydroisomerization. Sufficient quenching can inactivate the hydroisomerization catalyst bed. The hydroisomerization catalyst bed can be heated back to hydroisomerization temperature and can actively hydroisomerize again.

Process and apparatus for hydrocracking and hydroisomerizing a hydrocarbon stream

The invention relates to a hydrocarbon composition, which can be used as a fuel and/or fuel oil, containing a petroleum component (A) and a component of a biological origin (B), wherein the component of a biological origin is present in a quantity of up to 75% by volume with respect to the total composition. Said component of a biological origin (B) is prepared starting from a mix of a biological origin (C) containing esters of fatty acids, with possible aliquots of free fatty acids, by means of a process which comprises the following steps:

Hydrocarbon composition useful as a fuel and fuel oil containing a petroleum component and a component of a biological origin

A process for converting Fischer-Tropsch liquids and waxes into lubricant base stock and/or transportation fuels is disclosed. The process includes the steps of feeding a Fischer-Tropsch wax to a first isomerization unit to produce an isomerized Fischer-Tropsch wax product; combining a Fischer-Tropsch liquid with the isomerized Fischer-Tropsch wax product to create a mixture of the Fischer-Tropsch liquid and the Fischer-Tropsch wax product; and feeding the mixture to a fractionation column to separate the mixture into a lubricant base stock fraction and at least one transportation fuel fraction.

Process for converting fischer-tropsch liquids and waxes into lubricant base stock and/or transportation fuels

Methods and systems of processing a hydrocarbonaceous feed stock flows are provided. In one aspect, the method includes providing two or more hydroprocessing stages disposed in sequence, each hydroprocessing stage having a hydroprocessing reaction zone with a hydrogen requirement and each stage in fluid communication with the preceding stage. A hydrogen source is provided substantially free of hydrogen from a hydrogen recycle compressor. The hydrocarbonaceous feed stock flow is separated into an portions of fresh feed for each hydroprocessing stage, and then supplying the first portion of fresh feed with hydrogen from the hydrogen source in an amount satisfying substantially all of the hydrogen requirements of the hydroprocessing stages to a first hydroprocessing zone.

Multi-staged hydroprocessing process and system

In general, methods of hydroprocessing a hydrocarbonaceous feed stock are provided that do not use a costly recycle gas compressor, but are still able to use the more efficient reaction systems provided in a substantially three-phase hydroprocessing zone. The method combines a substantially liquid-phase hydroprocessing zone with the substantially three-phase hydroprocessing zone in a manner so that the hydrogen requirements for both reaction zones can be provided from an external source thereto without the use of a hydrogen recycle or recycle gas compressor to the substantially three-phase reaction zone.

Three-phase hydroprocessing without a recycle gas compressor

Two-stage hydroprocessing uses a common dividing wall fractionator. Hydroprocessed effluents from both stages of hydroprocessing are fed to opposite sides of the dividing wall.

Two-stage hydroprocessing apparatus with common fractionation

Crude tall oil is subjected to a distillation process that substantially removes impurities. The process produces a combined pitch and a distillate of free fatty acids and rosin acids from two vacuum columns. The distillate stream is amenable to further downstream hydroprocessing.

Process for separating crude tall oil for processing into fuels

Two-stage hydroprocessing with common fractionation

A process is provided to produce an ultra low sulfur diesel using a two stage hydrotreating reaction zone. The first stage hydrotreater may operate with a continuous liquid phase.

Two-stage hydrotreating process

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Palatine, IL, United States of America

John Anthony Petri