Thermally integrated process for the production of ethylene oxide from a flow of ethanol

Patent metadata

Field	Value
Publication number	US-9353074-B2
Application number	US-201414767184-A
Country	US
Kind code	B2
Filing date	Feb 6, 2014
Priority date	Feb 12, 2013
Publication date	May 31, 2016
Grant date	May 31, 2016

Abstract

Process for dehydrating an ethanol feed to ethylene then oxidating the ethanol to ethylene oxide, comprising vaporizing the feed and a flow of diluting water comprising recycled ethanol to produce a vaporized feed, dehydrating a mixture of vaporized feed and a vaporized flow of diluting water comprising ethanol, separating the dehydration effluent into ethylene and water effluents, purifying at least a portion of the water effluent and separating a flow of treated water and a flow of diluting water comprising ethanol, recycling and vaporizing at least a portion of the separated diluting water by partial or complete vaporization in an exchanger using heat exchange with a quench flow obtained from the oxidation, said quench flow, cooled, then recycled to the oxidation reactor(s), and oxidation of the ethylene in the effluent comprising ethylene into ethylene oxide, this oxidation using a tubular oxidation reactor cooled by vaporization of said quench flow.

First claim

The invention claimed is:

1. A process for the dehydration of an ethanol feed to ethylene then oxidation of the ethylene to ethylene oxide, comprising:
a) an optional step for preheating said ethanol feed to a temperature in the range 70° C. to 130° C. by heat exchange with the effluent obtained from step e);
b) an optional step for pre-treatment of the ethanol feed over an acidic solid operating at a temperature in the range 70° C. to 130° C. in order to produce a pre-treated ethanol feed;
c) a step for vaporization of a vaporization feed comprising said optionally pre-treated ethanol feed and at least a portion of the flow of diluting water comprising ethanol recycled in accordance with step h) to an exchanger by means of an exchange of heat with the effluent obtained from the last reactor of step e), said vaporization feed being introduced into said vaporization step at a pressure in the range 0.1 to 1.4 MPa so as to produce a vaporized feed;
d) a step for compressing and superheating said vaporized feed in a compressor so as to produce a compressed feed which is at the temperature for supplying to the dehydration section e);
e) a step for dehydration of a mixture comprising said compressed feed and the vaporized flow of diluting water comprising the ethanol obtained from step h), said mixture having a ratio of water to ethanol in the range 1 to 4 by weight, in at least one adiabatic reactor containing at least one dehydration catalyst and in which the dehydration reaction takes place, operating at an inlet temperature in the range 350° C. to 550° C. and at an inlet pressure in the range 0.3 to 1.8 MPa;
f) a step for separating the effluent obtained from the last adiabatic reactor of step e) into an effluent comprising ethylene at a pressure of less than 1.6 MPa and an effluent comprising water;
g) a step for purification of at least a portion of the effluent comprising water obtained from step f) and separation into at least a flow of treated water and a flow of diluting water comprising ethanol;
h) a step for recycling and vaporization of at least a portion of the flow of diluting water comprising ethanol obtained from step g) by partial or total vaporization in an exchanger using heat exchange with a quench flow obtained from oxidation step j) in a vaporization exchanger, said quench flow being cooled and then being recycled to the reactor or reactors of oxidation step j), said flow of at least partially vaporized diluting water comprising ethanol being recycled upstream of step e), the non-vaporized portion of the flow of treated water obtained from step g) being recycled to the inlet to vaporization step c);
i) a step for compression of the effluent comprising ethylene obtained from step f);
j) a step for oxidation of the ethylene comprised in the effluent comprising ethylene obtained from step i) into ethylene oxide, this oxidation step comprising at least one tubular oxidation reactor cooled by vaporization of said quench flow obtained from step h), said quench flow which has thus been reheated being recycled to step h).

2. The process according to claim 1 , in which the flow of diluting water comprising ethanol obtained from step h) is injected into the inlet to step e).

3. The process according to claim 1 , in which the flow of diluting water comprising ethanol obtained from step h) is injected into the inlet of a single phase gas/gas exchanger used in the compression and superheating step d).

4. The process according to claim 1 , in which said compressed feed is heated in a single phase type gas exchanger by means of an exchange of heat with the effluent obtained from the last adiabatic reactor of step e).

5. The process according to claim 1 , in which the compressed flow obtained from said step i) undergoes a purification.

6. The process according to claim 1 , in which the portion of the flow of diluting water comprising ethanol obtained from step g) is exchanging heat with the quench flow in step h) such that at least 50% of said flow of diluting water is vaporized at the outlet from said vaporization exchanger.

7. The process according to claim 1 , in which the pressure of the compressed feed is in the range 0.3 to 1.8 MPa.

8. The process according to claim 1 , in which the effluent obtained from the last adiabatic reactor of step e) is at a temperature in the range 270° C. to 450° C., and at a pressure in the range 0.2 to 1.6 MPa.

9. The process according to claim 1 , in which the dehydration step e) is carried out in one or two reactors.

10. The process according to claim 1 , in which said dehydration catalyst used in step e) is an amorphous acid catalyst or a zeolitic acid catalyst.

11. The process according to claim 1 , in which said ethanol feed comprises a percentage by weight of ethanol in the range 35% to 99.9% by weight.

12. The process according to claim 1 , in which the optional step b) for pre-treatment is conducted and supplemented by a pre-treatment using an anion exchange resin.

13. The process according to claim 1 , wherein the optional steps a) and b) are both conducted.

Assignees

• IFP Energies Nouvelles

Inventors

• Coupard Vincent
• Plennevaux Thomas

Classifications

• C07D303/04

  containing only hydrogen and carbon atoms in addition to the ring oxygen atoms · CPC title

• C07D301/03 Primary

  by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds · CPC title

• C07C1/24

  by elimination of water · CPC title

• C07D301/10

  with catalysts containing silver or gold · CPC title

• Y02P20/10

  Process efficiency · CPC title