ACID GAS RECOVERY UTILIZING ORGANIC ACID SALTED DIAMINE

• US 20130039829A1
• Filed: 08/09/2011
• Published: 02/14/2013
• Est. Priority Date: 08/09/2011
• Status: Abandoned Application

• Current Assignee: Cansolv Technologies Inc. (Shell Plc)
• Original Assignee: Cansolv Technologies Inc. (Shell Plc)
• Inventors: Ouimet, Michel
• Application Number:
  US13/205,982
• Publication Number:
  US 20130039829A1
• Time in Patent Office: Days
• US Class Current: 423/242.6
• CPC Class Codes: B01D 2252/2041 Diamines
• CPC Class Codes: B01D 2252/20447 containing a piperazine-ring
• CPC Class Codes: B01D 2252/205 Other organic compounds not covered by B01D2252/00 - B01D2252/20494
• CPC Class Codes: B01D 53/1425 Regeneration of liquid absorbents
• CPC Class Codes: B01D 53/1481 Removing sulfur dioxide or sulfur trioxide
• CPC Class Codes: Y02A 50/20 Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

A process for the capture of sulfur dioxide from a gaseous stream utilizing a regenerable diamine absorbent comprising a diamine and a weak organic acid.

Claims

1. A cyclic process for the removal of sulfur dioxide from a sulfur dioxide containing gas stream using an amine absorbent medium and for the regeneration of the absorbent medium comprising:

a) contacting the gas stream with a lean aqueous absorbing medium to absorb sulfur dioxide from the gas and to form a sulfur dioxide lean treated gas stream and spent absorbing medium, the lean aqueous absorbing medium comprising a sulfur dioxide diamine absorbent and an organic acid, the organic acid selected to convert the sulfur dioxide diamine absorbent to its half salt form;

b) steam stripping gaseous sulfur dioxide from the spent absorbing medium at a temperature to form a regenerated aqueous absorbing medium;

c) recovering the gaseous sulfur dioxide; and

,

d) recycling the regenerated aqueous absorbing medium to the contacting step.

2. The process as claimed in claim 1 wherein the lean aqueous absorbing medium has a pH of 4.5 to 6.5.

3. The process as claimed in claim 1 wherein the lean aqueous absorbing medium has a pH of 5 to 6.

4. The process as claimed in claim 1 wherein the organic acid has a pKa of 2.5 to 6.

5. The process as claimed in claim 1 wherein the organic acid has a pKa of 2.5 to 5.5.

6. The process as claimed in claim 1 wherein the organic acid has a pKa such that, at the pH of the lean aqueous absorbing medium, the organic acid is substantially in its basic form and at the pH of the spent absorbing medium, the organic acid is substantially in its acidic form.

7. The process as claimed in claim 1 wherein the organic acid comprises formic acid, glycolic acid, malonic acid, propanoic acid, succinic acid, phthalic acid, citric acid, adipic acid, tartaric acid, malic acid and mixtures thereof.

8. The process as claimed in claim 1 wherein the organic acid comprises formic acid, malonic acid, malic acid, tartaric acid, citric acid, adipic acid and mixtures thereof.

9. The process as claimed in claim 1 wherein the diamine has an amine with a lower pKa and an amine with a higher pKa and the higher pKa is above 6.5.

10. The process as claimed in claim 9 wherein the higher pKa is above 7.5.

11. The process as claimed in claim 1 wherein the diamine has an amine with a lower pKa and an amine with a higher pKa and the lower pKa is less than 5.0.

12. The process as claimed in claim 11 wherein the lower pKa is less than 4.0.

13. The process as claimed in claim 1 wherein the diamine comprises hydroxyethyl piperazine, bis-hydroxyethyl piperazine, piperazine, Hydroxyethylethylenediamine, bis-hydroxyethylethylenediamine and mixtures thereof.

14. The process as claimed in claim 1 wherein the diamine comprises bis-hydroxyethyl piperazine.

15. The process as claimed in claim 1 wherein the diamine has an amine with a lower pKa and an amine with a higher pKa and the aqueous absorbing medium has an organic acid concentration to neutralize the amine with a higher pKa prior to the lean aqueous absorbing medium contacting the sulfur dioxide containing gas.

16. The process as claimed in claim 1 wherein the lean aqueous absorbing medium has a heat stable salt concentration prior to contacting the sulfur dioxide containing gas that is less than 0.5 equivalents of acid per mole of diamine.

17. The process as claimed in claim 16 wherein the lean heat stable salt concentration prior to contacting the sulfur dioxide containing gas is less than 0.1 equivalents of acid per mole of diamine.