Ifp Energies Nouvelles

Compagnie Generale Des Etablissements Michelin

Olivier Thinon

Thierry Gauthier

Rejane Dastillung

Sophie Couderc

Vania Santos-Moreau

Vincent Coupard

Antoine Daudin

Alain Quignard

Raphael Huyghe

Anne Claire Pierron

Cyprien Charra

Adrien Mekki-Berrada

Frederic Favre

Mayara Azin Gondim Paiva

Anne Claire

The invention relates to a process of depolymerization of a polyester feedstock comprising PET, which comprises: a) a conditioning step; b) a glycolysis step in the presence of diol; c) a step of separation of the diol, producing at least a gaseous diol effluent, at least a liquid diol effluent and a liquid monomers effluent; g) a step of separating said liquid monomers effluent into a heavy impurities effluent and a prepurified monomers effluent, this step being conducted with a residence time of less than 10 min; e) a step of decolourizing the prepurified monomers effluent, in the presence of at least one adsorbent, and f) a diol purification step, which is supplied with at least a gaseous diol effluent and at least a liquid diol effluent, which are obtained from step c), and which produces a purified diol effluent and one or more impurities effluent(s).

Optimized depolymerization process by glycolysis of a polyester comprising polyethylene terephthalte

The invention relates to a process for producing a terephthalate polyester from at least one feedstock of polyester to be recycled, integrating a process of depolymerization, advantageously by glycolysis, of the polyester to be recycled in order to produce a diester intermediate compatible with the specifications of the polymerization steps and comprising an optimized system for recycling the streams.

Method for producing a polyester terephthalate incorporating a depolymerization method

A process for the production of a terephthalate polyester, containing a stage a) for preparing an esterification feedstock containing at least one mixing section fed with at least one terephthalic acid feedstock and one diester monomer feedstock, where the ratio of the total number of moles of diol units with respect to the total number of moles of terephthalate units introduced into the mixing section is between 1.0 and 2.0, the mixing section being operated at a temperature between 25° C. and 250° C. and at a pressure greater than or equal to 0.1 MPa, an esterification stage b) to produce at least one reaction effluent and one aqueous effluent, a polycondensation stage c) to obtain at least the terephthalate polyester and an effluent containing at least one diol monomer, and a stage d) of treatment of the diols to obtain a purified diol stream.

Process for the production of a terephthalate polyester from a monomer mixture comprising a diester

The present invention relates to an NCC process and an apparatus for producing light olefins and aromatics, wherein the C5+ fraction () of the cracking effluent is separated into a C5 fraction () recycled into the NCC reactor () and a C6+ fraction (), and wherein the C6+ fraction () is sent into an aromatics extraction unit () to produce an aromatics-enriched fraction () and a low-aromatics fraction ().

Apparatus and process for producing light olefins and aromatics by catalytic cracking

The present invention relates to an NCC process and an apparatus for producing light olefins and aromatics, wherein the fraction comprising ethane and/or propane () from the cracking effluent is sent at least partly into a steam cracking furnace (), fed with steam (), to produce a steam cracking effluent () comprising ethylene and/or propylene.

Apparatus and process for producing light olefins by catalytic and steam cracking

The invention relates to a process for producing butadiene from an ethanol feedstock comprising a step of converting ethanol into butadiene, a step of separating the reactants into a hydrated butadiene effluent, an impurities effluent and an ethanol-butadiene effluent, a separation step that separates the ethanol-butadiene effluent into a butadiene distillate and a contaminated reactants effluent, a step of purifying the butadiene by extractive distillation and an effluent treatment step.

Process for producing butadiene from ethanol integrated with extractive distillation

A subject-matter of the invention is a process for the depolymerization of a polyester feedstock comprising opaque PET, the said process comprising at least the stages of conditioning, of depolymerization and of separation of the diol and of separation of the liquid effluent rich in monomers, followed by a decolouration stage.

Process for the depolymerization of a polyester comprising opaque polyethylene terephthalate

The invention relates to a process for producing butadiene from an ethanol feedstock, comprising a step of converting the ethanol into butadiene, a distillation step, a step of washing with water, a butadiene purification step comprising at least one section for separating the 1-butene by extractive distillation and a final distillation section fed with the topped butadiene distillate, separating at the top a purified butadiene effluent and at the bottom a butene residue, and an effluent treatment step.

Process for producing butadiene from ethanol, comprising purification of a butadiene-loaded effluent by extractive distillation

The invention relates to a thermally-integrated method for producing butadiene from butanol that comprises at least the following steps:

Integrated method for producing butadiene from butanol

A process for the production of hydrocarbon products from a feed comprising at least one non-pre-treated bio-oil, comprising a first step for hydroreforming in the presence of hydrogen and a hydroreforming catalyst, used alone or as a mixture, to obtain at least one liquid effluent comprising at least one aqueous phase and at least one organic phase, a second step in which at least a portion of the organic phase of the effluent obtained from the first hydroreforming step is recycled to the first hydroreforming step with a recycle ratio equal to the ratio of the mass flow rate of said organic phase to the mass flow rate of the non-pre-treated bio-oil in the range 0.05 to 2 and in which the hydrocarbon effluent obtained from the hydrotreatment and/or hydrocracking step is not recycled to said first hydroreforming step.

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Roanne, France

Olivier Thinon