Isomerization with distillation and PSA recycle streams

• US 5,245,102 A
• Filed: 08/14/1992
• Issued: 09/14/1993
• Est. Priority Date: 11/29/1990
• Status: Expired due to Term

• Current Assignee: UOP Llc (Honeywell International Inc.)
• Original Assignee: UOP Llc (Honeywell International Inc.)
• Inventors: Symoniak, Martin F., Zarchy, Andrew S.
• Primary Examiner(s): McFarlane, Anthony
• Assistant Examiner(s): PHAN, NHAT
• Application Number:
  US07/929,237
• Time in Patent Office: 396 Days
• Field of Search: 585/734, 585/738, 585/748, 585/751
• US Class Current: 585/738
• CPC Class Codes: C07C 9/16 Branched-chain hydrocarbons
• CPC Class Codes: C10G 45/58 to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins C10G32/00 takes precedence; improving or increasing the octane number or aromatic content of naphtha C10G35/00
• CPC Class Codes: C10G 67/06 including a sorption process as the refining step in the absence of hydrogen

Abstract

An isomerization zone process is disclosed that combines a deisohexanizer with a PSA separation section to provide a product stream comprising methylbutane and dimethylbutane. The process combines a methylpentane and normal hexane recycle stream, a normal pentane recycle stream and a fresh feedstream to provide a combined feedstream that is charged to an isomerization zone. The effluent from the isomerization zone is stabilized and passed to a deisohexanizer. A sidecut stream carries the methylpentane and normal hexane recycle stream from the deisohexanizer. Hydrocarbons having a higher boiling point than the sidecut stream are withdrawn as a bottoms stream from the deisohexanizer. An overhead carries normal pentane, methylbutane and dimethylbutanes to the PSA separation section. An extract stream is recovered as the normal pentane recycle stream. The raffinate from the PSA provides a high octane isomerate stream comprising mainly methylpentane and dimethylbutanes.

Claims

1. A process for the isomerization of a feedstream comprising C₅ and C₆ hydrocarbons said process comprising:

(a) charging a first recycle stream and a second recycle stream into an isomerization zone, passing at least a portion of the C₅ and C₆ hydrocarbons of the feedstream into the isomerization zone directly or as a portion of at least one of said recycle streams, and contacting said recycle streams and said feedstream hydrocarbons with an isomerization catalyst at isomerization conditions effective to increase the branching of the hydrocarbons charged thereto and to produce an isomerization effluent stream comprising normal pentane, normal hexane, methylbutane, dimethylbutane, and methylpentane;

(b) passing at least a portion of said isomerization effluent stream to a deisohexanizer zone to distill said effluent stream and to produce an overhead stream comprising methylbutane, normal pentane, and dimethylbutane;

a bottoms stream having a boiling point at least greater than normal hexane; and

a sidecut stream comprising normal hexane and methylpentane;

(c) passing said overhead stream to a selective adsorption zone and therein contacting said overhead stream with an adsorbent at conditions effective to separate said overhead stream into an extract stream comprising normal hydrocarbons and a product stream comprising branched hydrocarbons;

(d) passing at least a portion of said extract stream and of said sidecut stream to step (a) as said first and second recycle streams; and

,

(e) recovering said product stream.

2. The process of claim 1 wherein said adsorption zone is operated under vapor phase conditions.

3. The process of claim 1 wherein said isomerization effluent is passed directly to a stabilizer operated at conditions selected to remove C₄ and lighter hydrocarbons from said effluent and the remainder of the effluent is passed directly to said deisohexanizer zone.

4. The process of claim 1 wherein the adsorbent in said adsorption zone comprises a 5A molecular sieve.

5. The process of claim 1 wherein said isomerization catalyst comprises from 0.01 to 0.25 wt. % platinum and from 2 to 10 wt. % of a chloride component and alumina.

6. The process of claim 1 wherein said adsorption zone comprises at least three operationally distinct beds of adsorbent and said beds are operated in, an adsorption mode wherein normal hydrocarbons are adsorbed from said overhead stream at a first pressure, a blowdown mode that cocurrently vents non-adsorbed gas components from and reduces the pressure in a bed that has just undergone adsorption to a second pressure, and a desorption mode that reduces the pressure in a bed that has just undergone blowdown mode to a third pressure while countercurrently recovering normal hydrocarbons.

7. The process of claim 1 wherein the entire feedstream is charged to step (a).

8. The process of claim 1 wherein at least a portion of the feedstream is charged to the deisohexanizer zone.

9. The process of claim 3 wherein at least a portion of the feedstream is charged to the stabilizer.

10. The process of claim 3 wherein the feedstream is charged to one of said stabilizer or said deisohexanizer zone, or directly to said isomerization zone.