Institut Francais Du Pe'trole

Procedes Petroliers Et Petrochimiques

Ifp Energies Nouvelles

Other

Institute Francais Du Petrole

Agip Petroli S.p.a.

Eni S.p.a. Division De Agip

Institut Francais Du Petrole Procedes Petroliers Et Petrochimques Eric

Eni S.p.a.

Eric Lenglet

Jean-Pierre Burzynski

Roland Huin

Alexandre Rojey

Paul Broutin

Jean-Marc Schweitzer

Luc Nougier

Nicolas Boudet

Frédéric Hoffmann

Yves Gougne

Franck Gaviot-Blanc

Herve Cazor

Christian R Busson

Fabrice Giroudiere

Stephane Bertholin

G&eacute;rard Courteheuse

Patrick Chaumette

Pierre Boucot

Jacques Alagy

Vincenzo Piccolo

Giuseppe Belmonte

Jean-Christophe Viguie

Gerard Courteheuse

G&eacute;rard Henri Martin

Stéphane Bertholin

Michel Cohen

Jean Luc Le Peutrec

Philippe Mege

Frédéric Hoffman

Fabrice Giroudière

A process for refining or pre-refining a crude oil P is described in which P is fractionated into several fractions, wherein partial oxidation of an asphaltenic residue R1 derived from P is carried out to produce a synthesis gas SG1 with an H/CO ratio of less than 1, steam cracking is carried out of an external light hydrocarbon fraction to produce a synthesis gas SG2 with a H/CO ratio of more than 3; SG1 and SG2 are mixed to produce a synthesis gas SG with a H/CO ratio in the range 1.2 to 2.5, and SG is converted by Fischer-Tropsch synthesis, then the waxes produced are converted into middle distillates. Preferably, a vacuum distillate VGO and/or a deasphalted oil DAO derived from P are hydrocracked mixed with the waxes. The invention also pertains to a facility for carrying out the process.

Process and facility for treatment of crude oil with asphaltenic residue conversion

The invention concerns a process for converting a stream of natural or associated gas into liquid fractions, comprising:

Process for converting gas into liquids with simplified logistics

A reconstituted non-asphaltenic oil Pa comprising at least 28% by weight of naphtha N, having a ratio R of 1.5 or more and a gasoline potential, POTg, in the range 47 to 70, in which: R=(0.9 N+0.5 VGO+)/(MD+0.1 VGO+), POTg=0.9N+0.5 VGO+, with in % by weight: N=naphtha: [30&#xb0; C./170&#xb0; C.]; MD=middle distillates: ]170&#xb0; C./360&#xb0; C.] and VGO+=fraction boiling above 360&#xb0; C. R indicates the relative gasoline potential of a non residual oil over middle distillates during its subsequent refining.

Non asphaltenic oil

The invention concerns a process for producing synthesis gas, SG, from hydrocarbons and/or recycled compounds. In the process: a stream comprising a first feed Fsupplemented with steam undergoes steam reforming in a multi-tube reactor-exchanger R having a shell and reaction tubes containing a steam reforming catalyst within the shell; the reaction tubes are heated by convection by circulating in the shell, in overall counter-current mode, a heating fluid HF external to the tubes, which fluid comprises a first combustion gas stream of a second feed F, then fluid HF is mixed, in 1 to 4 complementary combustion zones internal to the shell, with a third feed Fand a gas comprising oxygen, to increase the temperature of the HF, and then the mixture obtained circulates in R to heat the reaction tubes in a complementary manner; and SG is produced from the steam reforming effluent from Fand optionally part or all of the HF.

Process for producing synthesis gas by steam reforming in a reactor-exchanger

The process of the invention concerns a series of steps for preparing a solid lignocellulosic biomass type feed to supply a unit for gasification of that feed. The process employs at least one step for maturing the feed in the presence of a liquid hydrocarbon phase at a temperature in the range 250&#xb0; C. to 320&#xb0; C. for a residence time of at least 10 minutes, and milling the solid fragments which have thus been heat-treated in the presence of liquid hydrocarbon to obtain a suspension of solid in the divided form with a characteristic dimension of less than 150 micrometres. The invention also concerns a device for carrying out the process.

Process for converting biomass to produce synthesis gas

For producing synthesis gas, SG, from a hydrocarbon feed and optionally from recycled compounds, F, a first feed Fsupplemented with steam undergoes steam reforming in a multi-tube reactor-exchanger R comprising a plurality of reaction tubes () containing a steam reforming catalyst and a shell containing said tubes, to produce a first synthesis gas SG; reaction tubes () are heated principally by convection by circulating a fluid HF in the shell external to said tubes, in which HF is a staged partial oxidation stream with oxygen of a second feed Fat a pressure in the range 0.5 to 12 MPa, to produce a second synthesis gas SG; and the synthesis gas SG is produced by mixing SGand SG

Process for producing synthesis gas by steam reforming and partial oxidation

To facilitate operation of a facility for chemical conversion of a feed that comprises a reactor () containing a slurry constituted by at least one suspension of at least one solid in a liquid, a gas supply, and a circuit that is external of the reactor, for continuous movement of a slurry stream, wherein the external circuit withdraws slurry from the reactor from at least one point (A) and re-introduces at least a portion of the slurry at at least one other point (B), the facility is further provided with

Apparatus and process for optimising the circulation of a suspension in a facility comprising a three-phase reactor

Described are a reactor for carrying out a chemical conversion process in a catalytic bed with mechanism for supplying heat integrated into the reactor, and with a very compact reaction zone, combined with efficient use of the catalyst, and a process for converting a feed, such as a hydrocarbon feed, undergoing an endothermic reaction using the disclosed reactor.

Reactor for chemical conversion of a feed with added heat, and crosswise flow of feed and catalyst

Reactor device (R) for carrying out chemical reactions requiring heat exchange, the reactor is elongate along an axis (XX'), and has, at a first end, at least one orifice () for supplying at least one reactant, at an opposite end, at least one orifice () for evacuating the effluents formed, a plurality of heat exchangers () separated by at least one internal partition () and passages for circulating the reactant or reactants and/or effluents, provided between the heat exchangers and the internal partitions. The reactor (R) has at least one enclosure () made of refractory material providing heat insulation and containing a heat exchangers () and internal partitions (). The enclosure is contained in an envelope () to contain the reactant or reactants and/or effluents circulating inside the reactor.

Reactor device having an enclosure made of refractory material and a containment envelope for bringing about chemical reactions requiring heat exchange

Installation for chemical conversion of a feedstock by Fischer-Tropsch reaction comprising a reactor that contains a slurry constituted by at least one suspension of at least one solid in a liquid, a gas feed, a circuit, external to the reactor, of continuous circulation of a stream of slurry, whereby said slurry is drawn off at least one point (A) and reintroduced at least in part at least one other point (B), a section for separation of at least one slurry fluid that passes through said external circuit, whereby said installation also comprises: means allowing to shut down the circulation of said slurry in said circuit, means for introducing under pressure at least one fluid for purging the slurry that is contained in the circuit, and means allowing the circulation of the slurry in said external circuit under conditions such that the Reynolds number is greater than 2,500.

Device and process optimizing the circulation of a suspension in an installation comprising a Fischer-Tropsch reactor

Device and method for optimising the circulation of a suspension in a plant comprising a three-phase reactor

A reactor with integrated heat for carrying out a chemical conversion process in the presence of a gaseous diluent supplied through one or more ports at the upper and/or lower ends of a catalytic bed through which a feed moves substantially horizontally, and a process for converting a feed, such as a hydrocarbon feed in the reactor.

Reactor for chemical conversion of a feedstock in the presence of a diluent, with heat inputs and feedstock/catalyst cross-circulation

An elongate reaction vessel and process includes at least two stages in the vertical direction in which an endothermic or exothermic catalytic reaction is carried out and comprises: a catalytic reaction zone () per stage (); introducing () a reaction fluid to a stage adapted for transverse motion of the fluid across the whole vertical extent of the reaction zone; introducing and extracting the catalyst; a heat exchanger () for reaction fluids located inside the vessel between two successive reaction zones; means () for transporting reaction fluids from one stage to another preferably connected to the exchanger of the stage under consideration and to the inlet for reaction fluids of the subsequent stage; and means for recovering reaction fluids downstream of the last stage. The temperature variation in each zone and the temperature level are respectively adjusted by the thickness of each zone and by heat exchange.

Thin multi-stage catalytic reactor with internal heat exchanger, and use thereof

The invention concerns a process for converting hydrocarbons using at least one globally endothermic chemical reaction, in which a hydrocarbon feed successively traverses at least two reaction zones each containing at least one solid catalyst and comprising between said reaction zones an intermediate step, in a non catalytic zone, for reheating the stream (ST) from the first of the two reaction zones prior to its introduction into said second reaction zone, and in which said reheating is carried out in a heat exchanger, with heat transfer essentially by convection using a thermal fluid TF with a coking sensitivity index CS that is less than that of the stream ST, the difference in temperature &#x394;T between the temperature of the fluid TF at the inlet to the exchanger and the temperature of the stream ST at the heat exchanger outlet being less than 250&#xb0; C. The invention also concerns the use of said process for converting hydrocarbons and a unit for carrying out the process.

Process for endothermic conversion of hydrocarbons, its uses, and a unit for carrying out the process

Device for connecting a pipe that is intended for heating/or cooling a pressurized reactor and said reactor

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Rueil Malmaison, France

Eric Lenglet