Process for producing ethers by reacting olefins with alcohols

• US 4,267,393 A
• Filed: 11/08/1979
• Issued: 05/12/1981
• Est. Priority Date: 11/08/1978
• Status: Expired due to Term

• Current Assignee: Institut Francais Du Petrole (IFP Energies Nouvelles)
• Original Assignee: Institut Francais Du Petrole (IFP Energies Nouvelles)
• Inventors: Torck, Bernard, Hellin, Michel, Van Landeghem, Hugo, Vu, Quang D.
• Primary Examiner(s): Mars, Howard T.
• Application Number:
  US06/092,317
• Time in Patent Office: 551 Days
• Field of Search: 568/647
• US Class Current: 568/697
• CPC Class Codes: C07C 41/06 by addition of organic compounds only
• CPC Class Codes: C07C 43/04 Saturated ethers
• CPC Class Codes: C07C 43/046 Alkyl tert-alkyl ether, e.g. CH3OC(CH3)3

Abstract

An ether is prepared by reacting a selected olefin with an alcohol in a two reaction zone system: in the first reaction zone, the catalyst is dispersed in the liquid phase of the reactants and boiling of the mixture is avoided; in the second reaction zone, the catalyst is in a fixed bed. A cooled recycle stream is fed back to the first stage reactor. The catalyst is a sulfonated ion exchange resin in the acid form.

Claims

1. In a process for manufacturing ethers by contacting a mixture of at least one olefin having a double bond on a tertiary carbon atom and at least one alcohol with a sulfonated ion exchange resin catalyst in the acid form, the improvement comprising passing a liquid mixture of fresh reactants comprising said at least one olefin and said at least one alcohol, together with a liquid recycle stream as hereinafter defined at a feed rate of from 0.1 to 15 times the feed rate of the fresh reactants, upwardly through a first reaction zone containing a catalyst bed of particles of said sulfonated ion exchange resin in the acid form, at a temperature of from 60°

to 120°

C., said temperature being lower than the boiling temperature of the constituent of highest volatility in the mixture passing through the first reaction zone at the selected pressure, while maintaining a feed rate which is sufficient to expand the volume of said catalyst bed by at least 2% and to disperse the catalyst particles therein but insufficient to carry a substantial proportion of catalyst out of said first reaction zone, the contact time being selected to convert from 60 to 95% of said olefin;

discharging the liquid product mixture formed in the first reaction zone, cooling a first portion thereof, and recycling the cooled portion to the first reaction zone as said liquid recycle stream, and feeding a second portion of said liquid product mixture to a second reaction zone containing a fixed bed of said sulfonated ion exchange resin catalyst in the acid form, at a temperature of from 30°

to 70°

C., the temperature in the second zone being at least 10°

C. lower than the outlet temperature of the first reaction zone and lower than the boiling temperature of the constituent of highest volatility in the mixture passing through the second reaction zone at the selected pressure.

2. A process according to claim 1, wherein substantially adiabatic conditions are maintained in said first reaction zone, and at least the major part of the reaction heat evolved in the first reaction zone is extracted from the recycle stream outside of said first reaction zone.

3. A process according to claim 2, wherein the circulation rate of the liquid mixture of reactants in the first reaction zone is from 0.5 to 10 cm/sec and the size of the catalyst particles is from 0.05 to 5 mm.

4. A process according to claim 3, wherein the circulation rate of the liquid mixture of the reactants is from 1 to 4 cm/sec and the size of the catalyst particles is from 0.3 to 1.5 mm.

5. A process according to claim 1, wherein the recycle rate is 0.5 to 4 times the feed rate of the fresh charge of reactants.

6. A process according to claim 1, wherein the olefin is isobutene and its total conversion is at least 90%, with at least 3% in the second reaction zone.

7. A process according to claim 6, wherein the alcohol is methanol.

8. A process according to claim 6, wherein isobutene is supplied as a steam-cracking or catalytic cracking C₄ cut.

9. A process according to claim 8, wherein the C₄ cut also contains butadiene.

10. A process according to claim 1, wherein said at least one alcohol is at least one alkanol.

11. A process according to claim 1, wherein said at least one alcohol is at least one of methanol and ethanol.

12. A process according to claim 1, wherein the temperature in the second reaction zone is from 45°

to 60°

C.

13. A process according to claim 1, wherein the pressure in the first and second reaction zones is from 5 to 50 bars.

14. A process according to claim 6, wherein the temperature in the first reaction zone is from 80°

to 100°

C., and the conversion of isobutene in the first reaction zone is from 75 to 92%.

15. A process according to claim 1, wherein the olefin is at least one of 2-methyl-1-butene and 2-methyl-2-butene and its total conversion is at least 70%, with at least 3% in the second reaction zone.

16. A process according to claim 15, wherein the alcohol is methanol.

17. A process according to claim 15, wherein said at least one of 2-methyl-1-butene and 2-methyl-2-butene is supplied as a steam cracking or catalytic cracking C₅ cut.

18. A process according to claim 15, wherein the temperature in the first reaction zone is from 70°

to 90°

C., and the conversion in the first reaction zone is from 50 to 70%.