Regeneration of acid gas-containing treatment fluids

• US 8,303,685 B2
• Filed: 06/21/2004
• Issued: 11/06/2012
• Est. Priority Date: 07/22/2003
• Status: Expired due to Fees

• Current Assignee: Dow Global Technologies LLC (Dow, Inc.)
• Original Assignee: Dow Global Technologies LLC (Dow, Inc.)
• Inventors: Schubert, Craig N., Frank, Timothy C.
• Primary Examiner(s): Smith, Duane
• Assistant Examiner(s): WU, IVES J
• Application Number:
  US10/565,466
• Publication Number:
  US 20060178259A1
• Time in Patent Office: 3,060 Days
• Field of Search: 502/56, 423/228, 423/220, 423/229, 951/72, 951/81, 951/83, 951/93, 952/09, 952/35, 952/36, 951/78, 951/79
• US Class Current: 95/181
• CPC Class Codes: B01D 53/1425 Regeneration of liquid absorbents
• CPC Class Codes: B01D 53/1456 Removing acid components
• CPC Class Codes: B01D 53/1493 Selection of liquid materials for use as absorbents

Abstract

An improved acid gas regeneration and injection process wherein the separated acid gas stream emerging from a regenerator is compressed and injected into subsurface reservoir, the improvement comprising conducting the acid gas separation in the regenerator under pressure that exceeds 50 psia and does not exceed 300 psia.

Claims

1. A regeneration Process for an aqueous, acid gas-rich absorption Fluid comprising at least one nitrogen-based chemical absorbing Agent for an acid gas, which absorption Fluid contains a chemically absorbed acid gas comprising a) hydrogen sulfide, b) carbon dioxide or c) both of said gases, said Process comprising 1) stripping acid gas from the acid gas-rich absorption Fluid in a pressure Vessel operated at a pressure in excess of about 50 psia and below about 300 psia, wherein heat is supplied to the Fluid in the Vessel by a reboiler in a sufficient quantity that the Fluid is at a temperature from 294°

F. and below 400°

F. to desorb pressurized gases at a pressure in the range of about 50 psia to below about 300 psia that are carried to an outlet of the Vessel, and thereafter

     2) recovering an acid gas-rich gas stream from the outlet of the Vessel while maintaining the stream under a pressure in the range from 50 psia to 300 psia, wherein a control valve downstream from the outlet is used to control the operating pressure of the Vessel, and

     3) introducing said gas stream into a first stage compressor to increase the pressure and reduce by compression the volume of said recovered gas stream.

2. The process of claim 1 where at least one Agent in the treatment Fluid is an alkanolamine, comprising from 2 to 6 carbon atoms.

3. The process of claim 1 where at least one Agent is selected from the group consisting of ethanolamine;

diethanolamine;

diisopropanolamine;

triethanolamine;

N-methyldiethanolamine;

piperazine;

N-methylpiperazine;

N-hydroxyethylpiperazine;

2-(2-aminoethoxy)ethanol;

2-(2-text,-butylaminoethoxy)ethanol; and

2-amino-2-methyl-lpropanol.

4. The process of claim 2 where, included in the Fluid, is at least one co-solvent for acid gases selected from the group of:

a) methanol; and

b) individually or in combination C₁-C₃ alkyl mono- and di- ethers of ethylene, diethylene, triethylene, tetraethylene, pentaethylene, hexaethylene, heptaethylene, octaethylene, nonaethylene, and undecaethylene glycol; and

c) individually or in combination propylene carbonate;

1,3-dimethyl-3,4,5,6-tetrahydro-2(1H)-pyrimidinone;

sulfolane;

1-methyl-2-pyrrolidinone;

morpholine;

N-formylmorpholine; and

N-acetylmorpholine.

5. The process of claim 1, where the recovered gas stream is, after compression, disposed by injection to an ocean- or sea-bed or into a subterranean chamber or formation.

6. The process of claim 3 where, included in the Fluid, is at least one co- solvent for acid gases selected from the group of:

a) methanol; and

b) individually or in combination C₁-C₃ alkyl mono- and di- ethers of ethylene, diethylene, triethylene, tetraethylene, pentaethylene, hexaethylene, heptaethylene, octaethylene, nonaethylene, and undecaethylene glycol; and

c) individually or in combination propylene carbonate;

1,3-dimethyl-3,4,5,6-tetrahydro-2(1H)-pyrimidinone;

sulfolane;

1-methyl-2-pyrrolidinone;

morpholine;

N-formylmorpholine; and

N-acetylmorpholine.

7. The process of claim 1 wherein the stripping acid gas from the acid gas-rich absorption Fluid takes place in a pressure Vessel at a pressure in excess of about 55 psia and below about 300psia.

8. The process of claim 1 wherein the stripping acid gas from the acid gas-rich absorption Fluid takes place in a pressure Vessel at a pressure in excess of about 130 psia and below about 300 psia.

9. The process of claim 1 wherein the stripping acid gas from the acid gas-rich absorption Fluid takes place in a pressure Vessel at a pressure in excess of about 50 psia and below about 200 psia.

10. The process of claim 1 wherein the stripping acid gas from the acid gas-rich absorption Fluid takes place in a pressure Vessel at a pressure in excess of about 50 psia and below about 155 psia.