Process for producing 1,3-butadiene from a feedstock comprising ethanol

Patent metadata

Field	Value
Publication number	US-2016376206-A1
Application number	US-201415039881-A
Country	US
Kind code	A1
Filing date	Nov 28, 2014
Priority date	Nov 29, 2013
Publication date	Dec 29, 2016
Grant date	—

Abstract

Production of 1,3-butadiene ethanol, that is more than 50% of the total weight of feedstock:
A) conversion of feedstock and of ethanol effluent from separation B to a conversion effluent being a majority of 1,3-butadiene, water and ethylene, and to a hydrogen effluent, operating at a pressure between 0.1 and 1.0 MPa, a temperature between 300 and 500° C. in the presence of at least one catalyst; B) separation of conversion effluent originating from A and hydration effluent from C to an ethanol effluent, a butadiene effluent, a water effluent and an ethylene effluent; C) hydration of ethylene fed by ethylene effluent and/or water effluent both from separation B, to produce an ethanol hydration effluent then being recycled to separation B.

First claim

1 . Process for the production of 1,3-butadiene from a feedstock rich in ethanol, i.e. in which the ethanol represents more than 50% of the total weight of said feedstock, comprising at least:
A) A stage of conversion of at least said feedstock rich in ethanol and of the ethanol effluent originating from separation stage B to a conversion effluent comprising a majority of 1,3-butadiene, water and ethylene, and to a hydrogen effluent, operating at a pressure comprised between 0.1 and 1.0 MPa, at a temperature comprised between 300 and 500° C. in the presence of at least one catalyst; B) A stage of separation of at least said conversion effluent originating from A and the hydration effluent originating from C to at least an ethanol effluent, a butadiene effluent, a water effluent and an ethylene effluent; C) A stage of hydration of the ethylene fed at least by said ethylene effluent and/or said water effluent both originating from separation stage B, in order to produce a hydration effluent comprising ethanol, said hydration effluent then being recycled to the separation stage B.

2 . Process according to claim 1 , in which said stage A is operated at a pressure comprised between 0.1 and 0.5 MPa.

3 . Process according to claim 1 , in which said conversion stage A is operated in one reaction stage and in which said feedstock rich in ethanol is mixed with the ethanol effluent originating from the separation stage B before feeding said conversion stage A.

4 . Process according to claim 3 , in which said stage A is operated in the presence of a catalyst of zinc aluminate type or chromium-doped MgO—SiO 2 type, at a temperature comprised between 380 and 430° C.

5 . Process according to claim 1 , in which said stage A is operated in two reaction stages, the first stage making it possible to convert the ethanol to acetaldehyde in the presence of a catalyst consisting of a mixture of chromium oxide and copper oxide, or of any other suitable catalyst, the mass ratio of ethanol to acetaldehyde in the effluent of said first reaction stage being preferentially comprised between 2:1 and 4:1, said feedstock rich in ethanol feeding said first reaction stage and said ethanol effluent originating from said separation stage B feeding said second reaction stage, in a mixture with said effluent from said first reaction stage.

6 . Process according to claim 5 , in which the second reaction stage of said stage A is operated in the presence of a catalyst of silica type with an oxide of tantalum, zirconium or niobium, the second reaction stage of stage A being operated at a temperature comprised between 320 and 370° C., the first reaction stage of said stage A being operated at a temperature comprised between 200 and 300° C.

7 . Process according to claim 1 , in which the separation stage B is chosen from the stages of: distillation, cryogenic distillation, washing with solvent, extractive distillation, liquid-liquid extraction, passing through a sieve, membrane separation and the combinations of these stages.

8 . Process according to claim 1 , in which said stage C is an indirect hydration, in which, in a first reaction stage, the ethylene reacts in the presence of concentrated sulphuric acid at a reaction temperature comprised between 50 and 150° C., in a two-phase gas/liquid medium and in a second stage, the products formed in the first stage are hydrolyzed in order to form a majority of ethanol at a temperature comprised between 70 and 100° C.

9 . Process according to claim 1 , in which said stage C is a direct hydration operating in gas phase, at a reaction temperature comprised between 200 and 400° C., in the presence of a heterogeneous catalyst based on inorganic acids such as phosphoric acid deposited on supports based on silica.

10 . Process according to claim 1 , in which said feedstock rich in ethanol comprises acetaldehyde, the mass ratio of ethanol to acetaldehyde being comprised between 2:1 and 4:1.

11 . Process according to claim 1 , in which the purity of the ethylene flow feeding hydration stage C is comprised between 65 and 99.9% by weight.

12 . Process according to claim 1 , in which the purity of the ethylene flow feeding hydration stage C is comprised between 65 and 75% by weight.

Assignees

• Ifp Energies Now
• Michelin & Cie
• Michelin Rech Tech

Inventors

• Dastillung Rejane
• Cadran Nicolas
• Jacquin Marc
• Huyghe Raphael
• Fischer Beatrice

Classifications

• C07C29/04

  by hydration of carbon-to-carbon double bonds · CPC title

• C07C2523/26

  Chromium · CPC title

• C07C1/20 Primary

  starting from organic compounds containing only oxygen atoms as heteroatoms · CPC title

• C07C2521/08

  Silica · CPC title

• Y02P30/20

  using bio-feedstock · CPC title