Institut Francais Du Pe'trole

Eni S.p.a.

Institute Francais Du Petrole

Agip Petroli S.p.a.

Other

Institut Fran.cedilla.ais Du Petrole

Enitecnolgie Spa

Ifp Energies Nouvelles

Rhone-poulenc Chimie

Rhodia Chimie

Institut Francais Du P&eacute;trole

Lini Technologie S.p.a.

Agip Petroli

Enitechnologies E Uffici Di Via

Institut Franc&#xe1;is Du Petrole

Eric Benazzi

Slavik Kasztelan

Christophe Gueret

Nathalie George-Marchal

Pierre Marion

Christian Marcilly

Jean-Francois Joly

Nathalie Marchal-George

Fabio Alario

Alain Billon

Sylvie Lacombe

Patrick Briot

Tivadar Cseri

Jean-Francedillaois Joly

Samuel Mignard

Alain Forestiere

Johan Adriaan Martens

Elisabeth Merlen

Christine Travers

Patrick Euzen

Julia Magne-Drisch

Patrick Bourges

Jean-Fran&ccedil;ois Joly

Fr&eacute;d&eacute;ric Kolenda

Nathalie Ferrer

Jean-Yves Bernhard

Herve Cauffriez

Frederic Chaigne

Emmanuelle Guillon

Jean-Charles Viltard

Jean-Marie Basset

Jean-Louis Guth

Jean-Marie Deves

Jean-Claude Hipeaux

Lo&iuml;c Rouleau

Agnes Choplin

Jean Francois Joly

Jean Yves Bernhard

Avelino Corma Canos

Magalie Roy-Auberger

Michel Spagnol

Fabrice Diehl

Laurent Gilbert

Gil Mabilon

Bernard Torck

Philippe Caullet

Jean-Luc Duplan

Jerome Bonnardot

Loic Rouleau

Ronan Le Dred

Jocelyne Brendle

Jacques Baron

Cecile Plain

Olivier Martin

Nicolas Chouteau

Joao Miguel Da Silva

Maria Filipa Gomes Ribeiro

Daniel Saehr

Leon Lew

Vincent Coupard

Jean-Francois Le Page

Yves Chauvin

Thierry Gauthier

Gerard Paul Hotier

John Leonello Casci

Christophe Nedez

Jacques Alagy

Jean-Paul Euzen

Helene Olivier

Renaud Pontier

Pierre-Henri Bigeard

Andre Hirschauer

Henri Kessler

Albert Theolier

Maria Jose Diaz Cabanas

Carole Bobin

Herv&eacute; Cauffriez

Mathieu Pinault

Joaquin Martinez Triguero

Maryline Delage

Pierre Yout

Arnault Selmen

Sabine Valange

Zelimir Gabelica

Miguel Angel Camblor Fernandez

Rudy Parton

Jean Paul Gouzard

Ngi Suor Gnep

Serge Gautier

Bernadette Rebours

Fr&eacute;d&eacute;ric Chaigne

Nathalie Georges-Marchal

Roland Patrick Henney

Marion Claude

Sheena Maberly

Fre/ De/ Chaigne

Pierre-Yves Legoff

Michel Guisnet

Patricia Andy

Wim Souverijns

The present invention concerns an improved once-through process for hydrocracking hydrocarbon-containing feeds with high nitrogen contents, with partial elimination of ammonia, for example by a hot flash located between the hydrorefining zone and the hydrocracking zone. Said hot flash drum functions at a pressure close to that of the hydrorefining reactor and at a temperature in the range from 150&#xb0; C. to the hydrorefining reactor outlet temperature.

'Once through' process for hydrocracking hydrocarbon-containing feeds with high nitrogen contents

The invention relates to a process for preparing middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis, using a hydrocracking/hydroisomerization catalyst which comprises at least one hydrodehydrogenating element chosen from the group formed by the noble elements of Group VIII of the periodic table, a silica-alumina-based non-zeolitic support obtained from wherein the non-zeolitic silica-alumina based support was obtained from a process comprising starting from a mixture of a partially soluble alumina compound in an acid medium with a totally soluble silica compound or with a totally soluble combination of alumina and hydrated silica, the resultant moldable mixture is concentrated to form a moldable mixture, the resultant mixture is molded and the resultant molded article is subjected to a hydrothermal or thermal treatment.

Method for the production of middle distillates by hydroisomerisation et hydrocracking of charges arising from the Fischer-Tropsch method

A process for preparation of synthetic crude from a deposit of heavy crude, comprises: (a) the extraction of heavy crude by technology using steam; (b) the separation of crude extract and water; (c) the separation of crude into at least one light fraction and one heavy fraction; (d) the conversion of the heavy fraction of separation into a lighter product, said converted product, and a residue; (e) optionally, the partial or total hydrotreatment of the converted product and/or the light fraction (or fractions) obtained during the separation c), (f) the combustion and/or gasification of the conversion residue; the converted product and the light fraction (or fractions) for separation, optionally having been subjected to a hydrotreatment e), constituting the synthetic crude; said combustion allowing the generation of steam and/or electricity and said gasification allowing the generation of hydrogen; the steam and/or electricity thus generated being used for the extraction a) and/or the electricity and/or hydrogen thus generated being used for the conversion d) and/or the hydrotreatment e).

Integrated scheme of processes for extracting and treating an extra-heavy or bituminous crude

The invention relates to a process and installation for treating heavy petroleum feedstocks for producing a gas oil fraction that has a sulfur content of less than 50 ppm and most often 10 ppm that includes the following stages: a) mild hydrocracking in a fixed catalyst bed, b) separation from hydrogen sulfide of a distillate fraction that includes a gas oil fraction and a heavier fraction than the gas oil, c) hydrotreatment (including desulfurization) of said distillate fraction, and d) separation of a gas oil fraction with less than 50 ppm of sulfur. Advantageously, the heavy fraction is sent into catalytic cracking. The process preferably operates with make-up hydrogen that is brought to stage c), and very advantageously all of the make-up hydrogen of the process in introduced in stage c).

Process for converting heavy petroleum fractions for producing a catalytic cracking feedstock and middle distillates with a low sulfur content

A catalyst comprising at least one zeolite (molecular sieve) chosen from the group formed by the TON structure type zeolites (Theta-1, ZSM-22, ISI-1, NU-10 and KZ-2) and at least one zeolite chosen from the group formed by the zeolites (ZSM-48, EU-2, EU-11 and ZBM-30), at least one porous mineral matrix, at least one hydro-dehydrogenating element, preferably chosen from the elements of Group VIB and Group VIII of the periodic table, is used for the conversion of hydrocarbons, in particular for the reduction of the pour point of charges containing long (more than 10 carbon atoms) linear and/or slightly branched paraffins, in particular in order to convert, with a good yield, charges having high pour points to at least one cut having a low pour point and a high viscosity index for oil bases.

Catalyst and its use for improving the pour point of hydrocarbon charges

The invention concerns a process and apparatus wherein the paraffin effluent from the Fischer-Tropsch process is separated into a heavy fraction with an initial boiling point of 120-200&#xb0; C., said heavy fraction then optionally being hydrotreated then brought into contact with an amorphous hydroisomerization/hydrocracking catalyst that converts at least 80% by weight of the 370&#xb0; C.+ products into products with a boiling point of less than 370&#xb0; C. After distilling the hydrocracked fraction obtained to separate middle distillates, the residual heavy fraction is recycled.

Process for the production of middle distillates by hydroisomerisation and hydrocracking feeds from the Fischer-Tropsch process

The invention relates to a process for treating heavy petroleum feedstocks for producing a gas oil fraction that has a sulfur content of less than 50 ppm and most often 10 ppm that includes the following stages: a) ebulliated-bed catalytic hydrocracking, b) separation from hydrogen sulfide of a distillate fraction that includes a gas oil fraction and a heavier fraction than the gas oil, c) hydrotreatment of said distillate fraction, and d) separation of a gas oil fraction with less than 50 ppm of sulfur. Make-up hydrogen, preferably all make-up hydrogen, is to stage c). Advantageously, the heavier fraction from step (b) is subjected to catalytic cracking. The invention also relates to an installation that can be used for implementing this process.

Process for converting heavy petroleum fractions including an ebulliated bed for producing middle distillates with a low sulfur content

Process for transforming a gas-oil fraction that makes it possible to produce a fuel that has a quality according to stringent requirements in terms of sulfur content, aromatic compound content, cetane number, boiling point, T95, of 95% of the compounds and density, d15/4, at 15&#xb0; C. This process comprises a hydrorefining stage and a hydrocracking stage, whereby the latter uses a catalyst that contains at least one zeolite. The conversion of products that have a boiling point of less than 150&#xb0; C. is, throughout the two stages of hydrocracking and hydrorefining, less than 40% by weight and, for the hydrorefining stage, between 1 and 15% by weight. The temperature, TR2, of the hydrocracking stage is less than the temperature, TR1, of the hydrorefining stage, and the variation between temperatures TR1 and TR2 is between 0 and 80&#xb0; C.

Process for improving aromatic and naphtheno-aromatic gas oil fractions

A process for production of very high-quality base oils, and simultaneous production of high-quality middle distillates, comprises the successive stages of hydroisomerization and catalytic dewaxing. The hydroisomerization takes place in the presence of a catalyst containing at least one noble metal deposited on an amorphous acid support, the metal dispersion being less than 20%. The support is preferably an amorphous silica-alumina. The catalytic dewaxing takes place in the presence of a catalyst containing at least one hydrodehydrogenating element (Group VIII) and at least one molecular sieve chosen from ZBM-30, EU-2, and EU-11.

Flexible method for producing oil bases and distillates by hydroisomerization-conversion on a weakly dispersed catalyst followed by a catalyctic dewaxing

Process for transforming a gas oil fraction that makes it possible to produce a fuel that has a quality according to stringent requirements in terms of sulfur content, aromatic compound content, cetane number, boiling point, T95, of 95% of the compounds and density, d15/4, at 15&#xb0; C. This process comprises a hydrorefining stage and a subsequent stage, whereby the latter uses a catalyst that is selected from the group that consists of hydrorefining catalysts and catalysts that comprise at least one mixed oxide, a metal of group VIB, and a non-noble metal of group VIII. The conversion of products that have a boiling point of less than 150&#xb0; C. is, for the hydrorefining stage, between 1 and 15% by weight. The temperature, TR2, of the subsequent stage is less than the temperature, TR1, of the hydrorefining stage, and the variation between temperatures TR1 and TR2 is between 0 and 80&#xb0; C.

The invention concerns a process for producing middle distillates from effluents obtained from the Fischer-Tropsch process, comprising separating a heavy cut with an initial boiling point of 120-200&#xb0; C., hydrotreating said cut and fractionating the hydrotreated cut to obtain at least one intermediate fraction and at least one fraction that is heavier than the intermediate fraction. The intermediate fraction boils between Tand TTbeing in the range 120-200&#xb0; C. and Tbeing in the range 300-410&#xb0; C. The heavy and intermediate fractions are treated over a hydrocracking/hydroisomerisation catalyst and the effluents obtained are distilled. The invention also concerns a unit.

Process for the production of middle distillates by hydroisomerisation and hydrocracking feeds from the fischer-tropsch process

A hydrocracking catalyst containing at least one matrix, at least one zeolite chosen from the group formed by the zeolites ZBM-30, ZSM-48, EU-2, and EU-11, at least one Y zeolite, at least one hydro-dehydrogenating metal chosen from the group formed by the metals from Group VIB and Group VIII of the periodic table, optionally at least one element chosen from the group formed by phosphorus, boron and silicon, optionally at least one element from Group VIIA, and optionally at least one element from Group VIIB is used in a process of hydrocracking/hydroconversion of hydrocarbon charges.

Catalyst comprising at least one zeolite chosen from ZBM-30, SM-48 EU-2 and EU-11 and at least one Y zeolite and process of hydroconversion of hydrocarbon charges using such a catalyst

A catalyst comprising at least one ZBM-30 zeolite, synthesized in the presence of a particular structuring agent such as triethylenetetramine, at least one porous mineral matrix, at least one hydro-dehydrogenating element, preferably chosen from the elements of Group VIB and Group VIII of the periodic table, is used in order to improve the pour point of charges containing long (more than 10 carbon atoms) linear and/or slightly branched paraffins, in particular in order to convert, with a good yield, charges having high pour points to at least one cut having a low pour point and a high viscosity index for oil bases.

This invention relates to silico-aluminum substrates, catalysts, and the hydrocracking and hydrotreatment processes that use them. The catalyst comprises at least one hydro-dehydrogenating element that is selected from the group that is formed by elements of group VIB and group VIII of the periodic table and a non-zeolitic silica-alumina-based substrate that contains an amount of more than 5% by weight and less than or equal to 95% by weight of silica (SiO) and has the following characteristics:

Catalyst and process for hydrocracking hydrocarbon-containing feedstocks

For producing very high quality base stock and for simultaneously producing high quality middle distillates, successive hydroisomerisation and catalytic dewaxmg steps are employed wherein the hydroisomerisation is carried out in the presence of a catalyst containing at least one noble metal deposited on an amorphous acidic support, the dispersion of the metal being 20%-100%. The support is preferably an amorphous silica-alumina. Catalytic dewaxing is carried out in the presence of a catalyst containing at least one hydrodehydrogenating element (group VIII) and at least one molecular sieve selected from ZBM-30, EU-2 and EU-11.

Flexible method for producing oil bases and middle distillates with hydroisomerization-conversion followed by catalytic dewaxing

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Chatou, France

Eric Benazzi