Process for the recovery of heavy constituents from hydrocarbon gaseous mixtures

• US 4,657,571 A
• Filed: 06/19/1985
• Issued: 04/14/1987
• Est. Priority Date: 06/29/1984
• Status: Expired due to Fees

• Current Assignee: Snamprogetti S.p.A.
• Original Assignee: Snamprogetti S.p.A.
• Inventors: Gazzi, Luigi
• Primary Examiner(s): Capossela, Ronald C.
• Application Number:
  US06/746,331
• Time in Patent Office: 664 Days
• Field of Search: 62/11, 62/17, 62/23, 62/27, 62/38, 62/39
• US Class Current: 62/621
• CPC Class Codes: C07C 7/005 Processes comprising at least two steps in series
• CPC Class Codes: F25J 2200/04 in a dual pressure main 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 2200/76 Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
• CPC Class Codes: F25J 2200/78 Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
• CPC Class Codes: F25J 2200/80 using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
• 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 2230/60 the fluid being hydrocarbons or a mixture of hydrocarbons
• CPC Class Codes: F25J 2235/60 the fluid being (a mixture of) hydrocarbons
• CPC Class Codes: F25J 2240/02 Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
• CPC Class Codes: F25J 2270/02 Internal refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 3/0209 Natural gas or substitute natural gas
• CPC Class Codes: F25J 3/0233 separation of CnHm with 1 carbon atom 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

Abstract

A process is disclosed for the recovery of heavy constituents from high-pressure hydrocarbon gaseous mixtures comprising the steps of first cooling and partially condensing the gaseous mixture. The condensed liquid is then separated and fed to a fractionation column while the remaining non-condensed gaseous mixture is subject to turboexpansion. The liquid condensed on turboexpansion is then separated and fed to the fractionation column where the heavy constituents are recovered. The gases streaming from the fractionation column and those separated by turboexpansion are compressed, separately or together, up to the consignment pressure of the treated gas. This process is characterized in that the liquid condensed on turboexpansion is separated in a separator-absorber wherein, in addition to the condensed liquid, a liquid obtained by the absorption of the non-condensed heavy constituents is collected. Absorption is accomplished by an absorbent hydrocarbon oil, substantially free from the heavy constituents to be recovered. This oil is obtained from the cooling and partial condensation of the gases streaming from the fractionation column wherein a portion of the heavy constituents are removed by means of a dephlegmator and substantially compressed to a pressure higher than the pressure of the fractionation column.

Claims

1. Process for the recovery of heavy constituents from a high-pressure hydrocarbon gaseous mixture comprising the following steps:

(a) cooling and partial condensation of the hydrocarbon gaseous mixture;

(b) separation of the liquid condensed from the gaseous mixture and feeding of the same liquid to a fractionation column;

(c) turbo-expansion of non-condensed gaseous mixture;

(d) separation of the liquid condensed on turbo-expansion of the gaseous mixture and feeding of the same liquid to the said fractionation column, from whose bottom the heavy constituents are recovered;

(e) recompression both of the gases streaming from the fractionation column and of the gases separated in the step (d), separately or together, up to the consignment pressure of the treated gas,

characterized in that the separation of the liquid condensed on the turbo-expansion of the gaseous mixture is carried out in a separator-absorber in whose lower portion in addition to the condensed liquid a liquid is collected, which is obtained by means of the absorption of non-condensed heavy constituents by means of an absorbent oil constituted by a hydrocarbon liquid, substantially free from the heavy constituents to be recovered, obtained from the cooling and the at least partial condensation of the gases streaming from the fractionation column, previously deprived of at least a portion of the heavy constituents by means of a dephlegmator with which the same fractionation column is provided and compressed to a pressure above that of said fractionation column.

2. Process according to claim 1, wherein the gases streaming from the fractionation column are compressed before being sent to the dephlegmator in order to deprive them of at least a portion of the heavy constituents.

3. Process according to claim 1, wherein the liquid condensed on the turbo-expansion is pumped into the fractionation column at a pressure greater than that of the separator-absorber.

4. Process according to claim 1, wherein the absorbent hydrocarbon liquid is obtained from the cooling and from the at least partial condensation of the gases leaving the fractionation column together with the gases separated in the step (d) at least partly drawn from a suitable point of the recompression unit as per the step (e).

5. Process according to claim 4, wherein the gases at least partly drawn from a suitable point of the recompression unit as per the step (e) are further compressed before being cooled and partly condensed.

6. Process according to claims 4 or 5, wherein the gases at least partly drawn from a suitable point of the recompression unit before being cooled and partly condensed are under a pressure comprised within the range of from 20 to 100 atm, preferably of from 35 to 80 atm.

7. Process according to any one of the claims from 1 to 5, wherein the liquids obtained from the turbo-expansion and from the absorption by hydrocarbon oil are gas-stripped before being sent to the fractionation column.

8. Process according to claim 7, wherein the stripping gas is the raw gas at the plant inlet.

9. Process according to claim 8, wherein the raw gas entering the plant is turbo-expanded before being used as the stripping gas.

10. Process according to claim 9, wherein the power obtained from the turbo-expansion is used, possibly with the aid of another suitable driving unit, for the compression of the head gas of the fractionation column.

11. Process according to claim 8 wherein the stripping gas is in amount of from 2 to 25% by volume of the entering raw gas.

12. Process according to claim 8, wherein at least a portion of the striping gas is replaced by hydrocarbon vapours generated in a reboiler.

13. Process according to claim 7 wherein the stripping gas is in an amount of from 2 to 25% by volume of the entering raw gas.

14. Process according to claim 13, wherein the raw gas entering the plant is turbo-expanded before being used as the stripping gas.

15. Process according to claim 13, wherein at least a portion of the stripping gas is replaced by hydrocarbon vapours generated in a reboiler.

16. Process according to claim 7, wherein at least a portion of the stripping gas is replaced by hydrocarbon vapours generated in a reboiler.

17. Process according to any one of the claims from 1 to 5, wherein the turboexpander outlet pressure and the pressure of the absorber are comprised within the range of from 5 to 70 atm, preferably of from 15 to 50 atm.

18. Process according to any one of the claims from 1 to 5, wherein the pressure of the fractionation column is comprised within the range of from 5 to 45 atm, preferably of from 8 to 35 atm.