Processes integrating hydrocarbon cracking with metathesis for producing propene

Patent metadata

Field	Value
Publication number	US-11845705-B2
Application number	US-202117404379-A
Country	US
Kind code	B2
Filing date	Aug 17, 2021
Priority date	Aug 17, 2021
Publication date	Dec 19, 2023
Grant date	Dec 19, 2023

Abstract

Processes for producing olefins include passing a hydrocarbon feed to a hydrocarbon cracking unit that cracks the hydrocarbon feed to produce a cracker effluent, passing the cracker effluent to a cracker effluent separation system that separates the cracker effluent to produce at least a cracking C4 effluent including 1-butene, 1,3-butadiene, and isobutene, passing the cracking C4 effluent to an SHIU that contacts the cracking C4 effluent with hydrogen in the presence of a selective hydrogenation catalyst to produce a hydrogenation effluent having a 2-butenes concentration greater than or equal to the sum of the concentrations of 1-butene and isobutene. The processes include passing the hydrogenation effluent to a metathesis unit that contacts the hydrogenation effluent with a metathesis catalyst and a cracking catalyst downstream of the metathesis catalyst to produce a metathesis reaction effluent comprising at least propene.

First claim

What is claimed is:

1. A process for producing olefins, the process comprising:
passing a hydrocarbon feed to a hydrocarbon cracking unit that cracks at least a portion of the hydrocarbon feed to produce a cracker effluent;
passing the cracker effluent to a cracker effluent separation system that separates the cracker effluent to produce at least a cracking C4 effluent, where the cracking C4 effluent comprises at least 1-butene, 1,3-butadiene, and isobutene;
passing the cracking C4 effluent to a selective hydrogenation and isomerization unit that contacts the cracking C4 effluent with hydrogen in the presence of a selective hydrogenation catalyst at a temperature of from 60 degrees Celsius to 80 degrees Celsius and a pressure of from 20 bar (2,000 kilopascals) to 25 bar (2,500 kilopascals) to produce a hydrogenation effluent, where:
contacting the cracking C4 effluent with the hydrogen in the presence of the selective hydrogenation catalyst hydrogenates 1,3-butadiene to 1-butene, n-butane, or both and isomerizes at least a portion of the 1-butene to 2-butenes; and

passing the hydrogenation effluent to a metathesis unit that contacts the hydrogenation effluent with a metathesis catalyst and a cracking catalyst downstream of the metathesis catalyst to produce a metathesis reaction effluent comprising at least propene, where:
a concentration of 2-butenes in the hydrogenation effluent passed to the metathesis unit is greater than or equal to a sum of a concentration of 1-butene and a concentration of isobutene in the hydrogenation effluent;
the concentration of isobutene in the hydrogenation effluent passed to the metathesis unit is greater than or equal to 18 wt. %;
contacting with the metathesis catalyst causes metathesis of at least a portion of the 1-butene, 2-butenes, and isobutene in the hydrogenation effluent to produce a metathesis reaction product; and
contacting with the cracking catalyst causes at least a portion of C5+ olefins produced through metathesis to undergo cracking reactions to produce propene, ethylene, or both.

2. The process of claim 1 , where the concentration of 2-butenes in the hydrogenation effluent greater than or equal to the sum of the concentration of 1-butene and the concentration of isobutene in the hydrogenation effluent promotes formation of propene and suppresses formation of ethylene in the metathesis unit.

3. The process of claim 1 , where a concentration of isobutene in the hydrogenation effluent passed to the metathesis unit is from 18 wt. % to 50 wt. % per unit weight of the hydrogenation effluent.

4. The process of claim 1 , where the hydrogenation effluent has a mass ratio of 2-butenes to a sum of isobutene and 1-butene of from 1:1 to 9:1.

5. The process of claim 1 , where the selective hydrogenation catalyst comprises a transition metal supported on an alumina catalyst support.

6. The process of claim 5 , where the transition metal comprises palladium in an amount of from 0.01 weight percent to 1 weight percent based on the total weight of the selective hydrogenation catalyst.

7. The process of claim 1 , where the contacting the cracking C4 effluent with hydrogen in the presence of the selective hydrogenation catalyst further comprises contacting the cracking C4 effluent with the hydrogen in the presence of the selective hydrogenation catalyst at a weight hourly space velocity of the cracking C4 effluent of from 2 per hour to 4 per hour, a mass flow ratio of hydrogen to diene of from 0.1 to 3, or both of these conditions, where the mass flow ratio of hydrogen to diene is a mass flow rate of hydrogen to the hydrogenation and isomerization unit divided by a product of a weight fraction of dienes in the cracking C4 effluent and a mass flow rate of the cracking C4 effluent to the hydrogenation and isomerization unit.

8. The process of claim 1 , comprising passing the hydrogenation effluent directly from the selective hydrogenation and isomerization unit to the metathesis unit.

9. The process of claim 1 , where the hydrocarbon cracking unit comprises a high severity fluidized catalytic cracking unit and the process comprises contacting the hydrocarbon feed with a cracking catalyst under high-severity conditions to produce the cracker effluent comprising at least 1-butene, 1,3-butadiene, and isobutene, where the high-severity conditions comprise a temperature of greater than or equal to 500° C., a residence time of less than 3 seconds, and a cracking catalyst to hydrocarbon weight ratio of greater than 5:1.

10. The process of claim 1 , where the hydrocarbon cracking unit comprises a steam cracking unit and the process comprises contacting the hydrocarbon feed with at least steam at a temperature of from 700 degrees Celsius (° C.) to 900° C., where contacting causes at least a portion of the hydrocarbon feed to undergo steam cracking to produce the cracker effluent.

11. The process of claim 1 , further comprising separating the metathesis reaction effluent into a metathesis C4+ effluent and at least one olefin-containing effluent, the at least one olefin-containing effluent comprising at least one of ethylene, propene, or combinations of these and passing the metathesis C4+ effluent back to the hydrocarbon cracking unit.

12. The process of claim 1 , further comprising:
separating the metathesis reaction effluent into at least one olefin-containing effluent, a metathesis C4 effluent, and a metathesis C5+ effluent;
passing the metathesis C4 effluent to the selective hydrogenation and isomerization unit; and
passing the metathesis C5+ effluent to the hydrocarbon cracking unit.

13. The process of claim 1 , where:
the metathesis unit comprises a metathesis reactor comprising the metathesis catalyst and a cracking reactor comprising the cracking catalyst;
the cracking reactor is separate from and downstream from the metathesis reactor; and
the process further comprises:
passing a metathesis reactor effluent from the metathesis reactor to a first metathesis effluent separation unit that separates the metathesis reactor effluent into at least a metathesis ethylene effluent, a metathesis propene effluent, and a metathesis C4+ effluent;
passing the metathesis C4+ effluent to the cracking reactor disposed downstream of the first metathesis effluent separation system, where the cracking reactor contacts the metathesis reactor effluent with the cracking catalyst to produce a cracked metathesis effluent;
passing the cracked metathesis effluent to a second metathesis effluent separation unit downstream of the cracking reactor, where the second metathesis effluent separation unit separates the cracked metathesis effluent into an olefin containing stream and a metathesis C5+ effluent;
passing the metathesis C5+ effluent to the hydrocarbon cracking unit; and
passing the olefin containing stream to the first metathesis effluent separation unit.

14. The process of claim 1 , where the selective hydrogenation and isomerization unit comprises one or a plurality of fixed bed reactors.

15. The process of claim 1 , wherein the concentration of isobutene in the hydrogenation effluent passed to the metathesis unit is less than or equal to 30 wt. %.

16. The process of claim 1 , wherein the concentration of 1-butene in the hydrogenation effluent passed to the metathesis unit is greater than or equal to 10 wt. % and less than or equal to 30 wt. %.

Assignees

• Saudi Arabian Oil Co

Inventors

• Aljumah Furqan
• Shaikh Sohel
• Zhang Zhonglin

Classifications

• C10G2400/20

  C2-C4 olefins · CPC title

• C07C2523/44

  Palladium · CPC title

• C07C2523/30

  Tungsten · CPC title

• C07C2521/08

  Silica · CPC title

• C07C2521/04

  Alumina · CPC title