Process for producing ethylene oxide from ethane by oxidative dehydrogenation and epoxidation using a recycle reactor design

Patent metadata

Field	Value
Publication number	US-12492175-B2
Application number	US-202117908486-A
Country	US
Kind code	B2
Filing date	Mar 5, 2021
Priority date	Mar 9, 2020
Publication date	Dec 9, 2025
Grant date	Dec 9, 2025

Abstract

An ethylene oxide (EO) production process comprising (a) introducing a first reactant mixture (C 2 H 6 , C 2 H 4 , O 2 ) to a first reactor system to produce a first effluent stream (C 2 H 4 , C 2 H 6 , O 2 ), wherein the mole fraction of ethylene in first effluent stream is greater than in first reactant mixture; wherein the first reactor system is characterized by a first reactor system operating temperature of 270° C.-320° C.; wherein the first reactor system comprises oxidative dehydrogenation (ODH) stage(s); (b) introducing the first effluent stream to a second reactor to produce a second effluent stream (EO, C 2 H 4 , C 2 H 6 , O 2 ); (c) separating the second effluent stream into an EO product stream (EO) and recycle stream (C 2 H 4 , C 2 H 6 , O 2 ); wherein ethylene is not separated from recycle stream and/or first effluent stream; (d) recycling at least a portion of recycle stream to the first reactor system, and a optionally portion of recycle stream to the second reactor.

First claim

What is claimed is:

1 . An ethylene oxide (EO) production process comprising:
(a) introducing a first reactant mixture to a first reactor system to produce a first effluent stream;
wherein the first reactant mixture comprises ethane, ethylene, and oxygen; wherein the first effluent stream comprises ethylene, ethane, and oxygen; wherein the mole fraction of ethylene in the first effluent stream is greater than the mole fraction of ethylene in the first reactant mixture;
wherein the first reactor system is characterized by a first reactor system operating temperature; wherein the first reactor system operating temperature is defined as the average of first reactor system inlet temperature and first reactor system outlet temperature; wherein the first reactor system operating temperature is from about 270° C. to about 320° C.;
wherein the first reactor system comprises one or more oxidative dehydrogenation (ODH) stages; wherein each ODH stage is characterized by an ODH stage operating temperature; and wherein each ODH stage operating temperature is defined as the average of ODH stage inlet temperature and ODH stage outlet temperature for that particular ODH stage;
(b) introducing a second reactant mixture to a second reactor to produce a second effluent stream;
wherein the second reactant mixture comprises at least a portion of the first effluent stream;
and wherein the second effluent stream comprises EO, ethane, ethylene, and oxygen;
(c) separating at least a portion of the second effluent stream into an EO product stream and a recycle stream; wherein the EO product stream comprises at least a portion of the EO in the second effluent stream; and wherein the recycle stream comprises ethane, ethylene, and oxygen; and (d) recycling at least a portion of the recycle stream to the first reactor system in step (a) without separating ethylene from the recycle stream prior to the recycling, and optionally recycling a portion of the recycle stream to the second reactor in step (b).

2 . The process of claim 1 , wherein each ODH stage operating temperature is from about 270° C. to about 320° C.

3 . The process of claim 1 , wherein the first reactor system operating temperature and each ODH stage operating temperature are from about 270° C. to less than about 300° C.

4 . The process of claim 1 , wherein the first reactor system comprises a multitubular reactor, and wherein the multitubular reactor comprises a shell and a plurality of tubes disposed inside the shell.

5 . The process of claim 4 , wherein the plurality of tubes are substantially parallel to each other; wherein each tube comprises an ODH catalyst disposed therein; wherein the first reactant mixture is introduced to each of the plurality of tubes; wherein the multitubular reactor comprises a cooling medium contacting an inside shell surface and an outside surface of the tubes; wherein the cooling medium comprises water and/or heat transfer oil; and wherein the cooling medium maintains the first reactor system operating temperature within a range of from about 270° C. to about 320° C.

6 . The process of claim 4 , wherein each of the plurality of the tubes conveys a cooling medium contacting an inside surface of the tubes; wherein the cooling medium comprises water and/or heat transfer oil; wherein the first reactor system comprises an ODH catalyst disposed inside the shell and outside of the tubes; wherein the first reactant mixture is introduced inside the shell and outside of the tubes; and wherein the cooling medium maintains the first reactor system operating temperature within a range of from about 270° C. to about 320° C.

7 . The process of claim 5 , wherein the cooling medium comprises boiling water;
wherein the boiling water is characterized by a temperature of from about 260° C. to about 310° C.; and wherein the cooling medium maintains the first reactor system operating temperature within a range of from about 270° C. to less than about 320° C.

8 . The process of claim 5 , wherein the cooling medium comprises boiling water;
wherein the boiling water is characterized by a temperature of from about 260° C. to about 295° C.; and wherein the cooling medium maintains the first reactor system operating temperature within a range of from about 270° C. to less than about 300° C.

9 . The process of claim 1 , wherein the first reactor system comprises two or more ODH stages in series; wherein an ODH stage effluent is recovered from each ODH stage; wherein at least one ODH stage is substantially adiabatic; and wherein the ODH stage effluent is cooled prior to introducing it to a downstream ODH stage.

10 . The process of claim 9 further comprising (1) interstage effluent cooling between any two consecutive ODH stages in series; and/or (2) interstage ethane addition and/or interstage oxygen addition to the first reactor system.

11 . The process of claim 1 , wherein ethylene is not separated from the first effluent stream.

12 . The process of claim 1 , wherein a recycle split ratio is less than about 0.6; and
wherein the recycle split ratio is defined as the ratio of the volumetric flowrate of the portion of the recycle stream recycled to the first reactor system divided by the sum of the volumetric flowrate of the portion of the recycle stream recycled to the first reactor system and the volumetric flowrate of the portion of the recycle stream recycled to the second reactor.

13 . The process of claim 1 , wherein (1) the first reactant mixture is characterized by a molar ratio of ethylene to ethane of from about 1.3 to about 3.0; (2) the first effluent stream is characterized by an ethane concentration of from about 0.1 mol % to about 5 mol %; (3) the first reactor system is characterized by an ethane conversion of from about 60% to about 100%; (4) the first reactor system is characterized by an oxygen conversion of from about 30% to about 100%; (5) a concentration of ethane in the second reactant mixture and/or the recycle stream is from about 0.1 mol % to about 3 mol %; (6) the recycle stream is characterized by a combined concentration of ethane and ethylene of from about 15 mol % to about 60 mol %; or (7) any combinations of (1)-(6).

14 . The process of claim 1 further comprising withdrawing a portion of the recycle stream as a purge stream; wherein the purge stream is characterized by a purge ratio of from about 0.0001 to about 0.005; and wherein the purge ratio is defined as the ratio of the volumetric flowrate of the purge stream divided by the volumetric flowrate of the recycle stream.

15 . An ethylene oxide (EO) production process comprising:
(a) introducing a first reactant mixture to an oxidative dehydrogenation (ODH) reactor system to produce a first effluent stream; wherein the first reactant mixture comprises ethane, ethylene, and oxygen; wherein the first effluent stream comprises ethylene, ethane, and oxygen; wherein the mole fraction of ethylene in the first effluent stream is greater than the mole fraction of ethylene in the first reactant mixture;
wherein the ODH reactor system is a multitubular reactor; wherein the multitubular reactor comprises a shell and a plurality of tubes disposed inside the shell; wherein the plurality of tubes are substantially parallel to each other; wherein each tube comprises an ODH catalyst disposed therein; wherein the first reactant mixture is introduced to each of the plurality of tubes;
wherein the multitubular reactor comprises a cooling medium contacting an inside shell surface and an outside surface of the tubes; wherein the cooling medium comprises boiling water; and wherein the

Assignees

• Broekhuis Robert Roger
• Gautam Pankaj Singh
• Gu Tian
• SARSANI Vidya Sagar Reddy
• Sabic Global Technologies Bv

Inventors

• Broekhuis Robert Roger
• Gautam Pankaj Singh
• Gu Tian
• SARSANI Vidya Sagar Reddy

Classifications

• C07D303/04

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

• C07D301/08 Primary

  in the gaseous phase · CPC title