Process for N-butanizing field butane feedstock to thermal crackers

Patent metadata

Field	Value
Publication number	US-11358916-B2
Application number	US-201917047001-A
Country	US
Kind code	B2
Filing date	Apr 23, 2019
Priority date	Apr 27, 2018
Publication date	Jun 14, 2022
Grant date	Jun 14, 2022

Abstract

Described is a process for producing field butane. The process includes increasing the n-butane concentration in field butane. The process may include a concentration process that includes distillation and a thermal cracking process.

First claim

The invention claimed is:

1. A method of increasing n-butane concentration in field butane, the method comprising:
subjecting a feed stream, comprising primarily n-butane and isobutane collectively, to a concentrating process, the concentrating process comprising distilling the feed stream in one or more distillation columns to produce a first product stream comprising primarily n-butane and a second product stream comprising methane, ethane, and propane; and
cracking, in a thermal cracker, the first product stream to produce a third product stream comprising primarily ethylene and a fourth product stream comprising primarily n-butane; and
recycling, from the thermal cracker, at least some of the fourth product stream to the one or more distillation columns;
wherein the concentrating process comprises:
distilling, in a first distillation column, a combined stream that comprises a mixture of the feed stream and a recycle stream comprising primarily isobutane to produce a bottoms stream comprising primarily n-pentane, an intermediate stream comprising primarily n-butane, and an overhead stream comprising primarily isobutane;
combining the intermediate stream and the bottoms stream to produce the first product stream;
isomerizing the overhead stream in a reactor to convert at least some of the isobutane in the overhead stream to n-butane; and
distilling effluent from the reactor, in a second distillation column, to form the recycle stream and the second product stream.

2. The method of claim 1 , wherein the isomerizing includes mixing the overhead stream with hydrogen to form a combination and contacting the combination with a catalyst under reaction conditions to isomerize at least some of the isobutene to n-butane.

3. The method of claim 2 , wherein the catalyst does not include zeolite and is a selection from the list consisting of: sulfated zirconia, platinum on alumina dosed with perchloroethylene or other chlorinating agent, flouridized catalyst, and combinations thereof.

4. The method of claim 2 , wherein the reaction conditions include a reaction temperature of 130 to 300° C., a pressure of 10 to 30 bar and GHSV of 4 to 5.5.

5. The method of claim 1 , wherein effluent from the reactor comprises 42 mol. % to 52 mol. % isobutane and 35 mol. % to 45 mol. % n-butane.

6. The method of claim 1 , wherein the recycle stream comprises 48 mol. % to 58 mol. % isobutane and 42 mol. % to 52 mol. % n-butane.

7. The method of claim 1 , wherein the n-butane/isobutene mol. ratio in field butane is in a range a range 1.8 to 2.8 and wherein the first product stream comprises 85 mol. % to 95 mol. % n-butane.

8. The method of 1 , wherein the feed stream comprises 62 mol. % to 72 mol. % n-butane and 24 mol. % to 34 mol. % isobutene and wherein the first product stream comprises 85 mol. % to 95 mol. % n-butane.

9. The method of 1 , wherein the feed stream comprises 94 mol. % to 98 mol. % n-butane and isobutane collectively.

10. The method of 1 , wherein the feed stream further comprises n-pentane.

11. The method of 1 , wherein the second product stream further comprises 5 mol. % to 15 mol. % methane, 15 mol. % to 25 mol. % ethane, and 65 mol. % to 75 mol. % propane.

12. The method of claim 1 , wherein the overhead stream comprises 94 mol. % to 98 mol. % isobutane and 2 mol. % to 6 mol. % propane.

13. The method of claim 1 , wherein the intermediate stream comprises 96 mol. % to 100 mol. % n-butane.

14. The method of claim 1 , wherein the bottoms stream comprises 96 mol. % to 100 mol. % n-pentane.

15. The method of claim 1 , wherein the fourth product stream comprises 98 mol. % to 99.8 mol. % n-butane.

16. The method of claim 1 , wherein the at least some of the fourth product stream is recycled to the first distillation column.

17. The method of claim 1 , further comprising
identifying a composition crossover point in the first distillation column;
identifying a tray closest to the composition crossover point in the first distillation column;
withdrawing a stream from above the identified tray;
heating the withdrawn stream; and
reinjecting the heated stream to a selected tray below the identified tray.

18. The method of claim 1 , further comprising:
identifying a composition crossover point in the first distillation column;
identifying a tray closest to the composition crossover point in the first distillation column;
withdrawing a stream from below the identified tray;
cooling the withdrawn stream; and
reinjecting the cooled stream to a selected tray above the identified tray.

19. The method of claim 2 , further comprising:
identifying a composition crossover point in the first distillation column;
identifying a tray closest to the composition crossover point in the first distillation column;
withdrawing a stream from below the identified tray;
cooling the withdrawn stream; and
reinjecting the cooled stream to a selected tray above the identified tray.

Assignees

• Sabic Global Technologies Bv

Inventors

• Bodas Vijay Dinkar
• Al-Otaibe Sultan
• Leal Guillermo
• Ansari Mohammed Bismillah

Classifications

• C07C7/04 Primary

  by distillation · CPC title

• C07C5/2727

  with hydrides or organic compounds (C07C5/2718 takes precedence) · CPC title

• C07C2531/02

  containing organic compounds or metal hydrides · CPC title

• C07C4/04 Primary

  Thermal processes {(C07C4/025 takes precedence)} · CPC title

• B01D3/146

  Multiple effect distillation · CPC title