Hybrid condensation-absorption olefin recovery

• US 5,453,559 A
• Filed: 04/01/1994
• Issued: 09/26/1995
• Est. Priority Date: 04/01/1994
• Status: Expired due to Term

• Current Assignee: MW Kellogg Limited (KBR Incorporated)
• Original Assignee: MW Kellogg Limited (KBR Incorporated)
• Inventors: Phillips, Christopher L., Verma, Vijender K.
• Primary Examiner(s): McFarlane, Anthony
• Assistant Examiner(s): PHAN, NHAT
• Application Number:
  US08/221,616
• Time in Patent Office: 543 Days
• Field of Search: 585/809, 95/42, 62/24
• US Class Current: 585/809
• CPC Class Codes: C10G 5/04 with liquid absorbents
• CPC Class Codes: C10G 70/06 by gas-liquid contact
• CPC Class Codes: F25J 2200/38 using pre-separation or distributed distillation before a main column system, e.g. in a at least a double column system
• CPC Class Codes: F25J 2200/74 Refluxing the column with at least a part of the partially condensed overhead gas
• CPC Class Codes: F25J 2205/02 using simple phase separation in a vessel or drum
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2205/50 using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
• CPC Class Codes: F25J 2210/12 Refinery or petrochemical off-gas
• CPC Class Codes: F25J 2215/62 Ethane or ethylene
• CPC Class Codes: F25J 2215/64 Propane or propylene
• CPC Class Codes: F25J 2270/04 Internal refrigeration with work-producing gas expansion loop
• CPC Class Codes: F25J 2270/12 External refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 2270/60 Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
• CPC Class Codes: F25J 2270/902 Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.
• CPC Class Codes: F25J 3/0219 Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
• CPC Class Codes: F25J 3/0233 separation of CnHm with 1 carbon atom or more
• CPC Class Codes: F25J 3/0238 separation of CnHm with 2 carbon atoms or more
• CPC Class Codes: F25J 3/0242 separation of CnHm with 3 carbon atoms or more
• CPC Class Codes: F25J 3/0247 separation of CnHm with 4 carbon atoms or more
• CPC Class Codes: F25J 3/0252 separation of hydrogen production of hydrogen containing gas in general C01B3/00, e.g. separation of hydrogen or hydrogen containing gases form gaseous mixtures at low temperatures C01B3/506

Abstract

A hybrid condensation-absorption process and unit is disclosed for the recovery of olefins. A mixed-component stream containing hydrogen, methane and olefins is compressed and refrigerated against propylene refrigerant to partially condense the stream. The condensate is stripped of volatile components and fed to a fractionation unit such as a deethanizer. The volatile components stripped from the condensate and the non-condensed vapor from the mixed-component stream are fed to a solvent absorption unit to remove olefins which are absorbed in the solvent. The olefins-rich solvent is regenerated to recover olefins and lean solvent. The lean solvent is recirculated to the absorption unit. The olefins recovered from regeneration of the solvent are fed to the fractionation unit along with the pre-stripped condensate. Vapor from the absorption unit is cryogenically processed to recover a crude hydrogen product, a fuel gas product and residual olefins which can be recycled to the absorption unit. The hybrid process eliminates the need for low temperature (ethylene) refrigeration equipment, generally required by conventional condensation-based olefins recovery technology, and substantially reduces the solvent recirculation rate to the absorption unit and eliminates hydrogen expansion as compared to conventional absorption-based technology.

Claims

1. A hybrid condensation-absorption process for separating and recovering olefins from a cracking furnace effluent, comprising the steps of:

(a) refrigerating a mixed-component stream containing hydrogen, methane and olefins to form vapor and condensate streams;

(b) fractionating the condensate stream from step (a) to obtain an overhead stream comprising hydrogen, methane and olefins and a bottoms product stream comprising olefins essentially free of hydrogen and methane;

(c) contacting the vapor stream from step (a) and the overhead stream from step (b) with an olefins-lean solvent to absorb olefins in the solvent and form a vapor stream of hydrogen and methane substantially free of olefins and an olefins-rich solvent stream;

(d) regenerating the olefins-rich solvent stream to form the olefins-lean solvent stream for recycle to step (c) and an olefins stream essentially free of solvent; and

(e) fractionating the olefins streams from steps (b) and (d) to obtain one or more purified olefin product streams.

2. The process of claim 1, wherein the refrigeration in step (a) is primarily against propylene refrigerant.

3. The process of claim 1, wherein a major portion of the mixed-component stream is condensed in step (a).

4. The process of claim 1, wherein step (a) occurs at a pressure above 2.5 MPa.

5. The process of claim 1, wherein the solvent contacting step (c) comprises the steps of:

(1) contacting the vapor stream from step (a) with a first portion of the olefins-lean solvent from step (d) to form a first methane vapor stream essentially free of olefins and a first intermediate olefins-enriched solvent stream;

(2) contacting the overhead stream from step (b) with a second portion of the lean solvent from step (d) to form a second methane vapor stream essentially free of olefins and a second intermediate olefins-enriched solvent stream; and

(3) stripping methane from the intermediate solvent streams to form the olefins-rich solvent stream for thermal regeneration in step (d).

6. The process of claim 5, wherein the steps (2) and (3) of step (c) comprise the steps of:

(A) feeding the overhead stream from step (b) and the first intermediate solvent stream from step (1) to a mid-column feed zone of a solvent stripping column having an absorption zone above the feed zone and a stripping zone below the feed zone;

(B) feeding the second portion of the lean solvent to the absorption zone;

(C) heating the stripping zone; and

(D) recovering the olefins-rich solvent stream from the stripping zone for regeneration in step (d).

7. The process of claim 5, wherein:

step (b) comprises the steps of;

(A) feeding the condensate from step (a) to a feed zone of a prestripping column having a solvent absorption zone receiving vapor from the feed zone, and a heated stripping zone below the feed zone in fluid communication therewith; and

(B) recovering the bottoms product stream from said stripping zone;

step (2) comprises the steps of;

(C) feeding the second portion of the lean solvent from step (d) to an upper portion of the solvent absorption zone of the prestripping column;

(D) recovering the second methane vapor stream overhead from the solvent absorption zone of the prestripper column; and

(E) recovering the second intermediate solvent stream from a lower portion of the absorption zone of the prestripping column; and

step (3) comprises the steps of;

(F) feeding the intermediate solvent streams from steps (1) and (E) to a feed zone of a solvent stripping column having an absorption zone above the feed zone of the solvent stripping column, and a heated stripping zone below the feed zone of the solvent stripping column;

(G) feeding a third portion of the lean solvent from step (d) to an upper portion of the absorption zone of the solvent stripping column;

(H) recovering a third methane vapor stream overhead from the absorption zone of the solvent stripping column; and

(I) recovering the olefins-rich solvent stream from a lower portion of the stripping zone of the solvent stripping column for regeneration in step (d).

8. The process of claim 5, wherein the contacting step (1) is effected in a propylene-refrigerated absorption zone.

9. The process of claim 5, wherein the stripping step (3) is effected in a stripping zone at least partially heated by cooling propylene refrigerant.

10. A method for expanding the production capacity of an olefins recovery plant wherein a mixture of olefins, methane and hydrogen is cooled against propylene refrigerant to condense a portion of the olefins and produce an intermediate vapor stream, and the intermediate vapor stream is cooled against ethylene refrigerant to condense out substantially all of the remaining olefins from the intermediate stream, where ethylene refrigerant capacity is a bottleneck, comprising:

installing a solvent absorption/regeneration unit;

diverting at least a portion of the intermediate vapor stream to an absorption zone of the solvent absorption/regeneration unit;

wherein the diverted vapor is contacted with lean solvent to absorb olefins into the solvent to form a vapor product stream essentially free of olefins and an olefin-enriched solvent stream;

regenerating the olefins-enriched solvent stream in a regeneration zone of the solvent absorption/regeneration unit to form an olefins stream, essentially free of solvent and methane, and a lean solvent stream for recycle to the absorption unit;

feeding the olefins stream from the regeneration zone to an olefin fractionation unit.