Ifp Energies Nouvelles

Total Raffinage Chimie

Institut Francais Du Pe'trole

Totalenergies Onetech

Stephane Bertholin

Alexandre Rojey

Christophe Boyer

Florent Guillou

Mahdi Yazdanpanah

Ann Cloupet

Fabrice Giroudiere

Eric Lenglet

Beatrice Fischer

Aziz A Sattar

Tiago Sozinho

Hélène Stainton

Benjamin Amblard

Sina Tebianian

Airy Tilland

Ann Forret

William Pelletant

Jerome Colin

Tedd Knowlton

Surya Reddy Karri

The present invention relates to a device and a method for chemical looping combustion, for which the end of the intake duct () opening out within the chamber of the separator () is inclined with respect to a horizontal plane (H).

Device and method for chemical looping combustion, having a particle separator provided with an inclined intake duct

The invention relates to a CLC plant for the combustion of solid hydrocarbon feedstocks generating particles of unburnt residues, comprising a solid/solid separator above the combustion reactor in order to efficiently separate the particles of the oxygen-carrying solid from the particles of unburnt residues contained in the gas/solid mixture () exiting from the combustion reactor. The chamber () of the solid/solid separator, the combustion reactor and the inlet () for the gas/solid mixture () of the chamber have a parallelepiped shape. The inlet () is equipped at its top with means () for distribution of said gas/solid mixture in the chamber which extend over the entire length of the inlet, improving the solid/solid separation.

CLC facility comprising a solid/solid separator with means for distributing a gas-solid mixture

The invention concerns a CLC process, and its installation, producing high purity dinitrogen, comprising:

CLC process and installation with the production of high purity nitrogen

The invention relates to a method and to a plant for chemical looping oxidation-reduction combustion (CLC) of a gaseous hydrocarbon feed, for example natural gas essentially containing methane. According to the invention, catalytic steam reforming of the feed is performed between two successive feed combustion steps on contact with an oxidation-reduction active mass in form of particles. The reforming catalyst is arranged in a fixed bed in an intermediate reforming zone () between the two reduction zones () where the two combustion steps are conducted.

Method and plant for chemical looping oxidation-reduction combustion of a gaseous hydrocarbon feedstock with intermediate catalytic steam reforming of the feed

In a method and a plant for chemical looping oxidation-reduction combustion (CLC) of a gaseous hydrocarbon feed, for example natural gas essentially containing methane, catalytic reforming of the feed is performed within the reduction zone where combustion of the feed is conducted on contact with an oxidation-reduction active mass in form of particles. The reforming catalyst comes in form of untransported fluidized particles within the reduction zone. The catalyst thus confined in the reduction zone does not circulate in the CLC loop.

Method and plant for chemical looping oxidation-reduction combustion of a gaseous hydrocarbon feedstock with in-situ catalytic reforming of the feed

The invention relates to a plant and to a method for chemical looping oxidation-reduction combustion of a gaseous hydrocarbon feed, for example natural gas essentially containing methane. According to the invention, catalytic pre-reforming of the feed is performed in a pre-reforming zone comprising a fixed reforming catalyst, while benefiting from a heat transfer between the reduction or oxidation zone of the chemical loop and the pre-reforming zone adjoining the reduction or oxidation zone. Pre-reforming zone () and oxidation zone () or pre-reforming zone () and reduction zone () are thus thermally integrated within the same reactor () while being separated by at least one thermally conductive separation wall ().

Plant and method for chemical looping oxidation-reduction combustion of a gaseous hydrocarbon feedstock with catalytic pre-reforming of the feed

The present invention describes a novel reactor adapted for carrying out chemical reactions at temperatures of up to 1600&#xb0; C., and at pressures of up to 100 bars. The reactor of the invention has two vessels surrounding the reaction zone, an inner vessel constituted by a refractory material and an outer vessel surrounding the inner vessel and constituted by an insulating material.

Reactor for carrying out very high temperature and high pressure reactions

The invention concerns an exchanger-reactor () comprising:

Internal combustion exchanger-reactor for fixed bed endothermic reaction

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

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

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Chaponost, France

Stephane Bertholin