Method and system for treatment of a gas stream that contains carbon dioxide
A method for separating carbon dioxide (CO 2 ) from a gas stream is disclosed, in which the gas stream is reacted with a lean aminosilicone solvent in an absorber, resulting in a rich aminosilicone solvent that is then treated in a desorber to release the CO 2 and regenerate lean aminosilicone solvent in a desorption reaction. The regenerated solvent is directed into a steam-producing, indirect heat exchanger that is configured to supply steam to the desorber at a temperature high enough to augment the desorption reaction. Also, selected amounts of make-up water are added to the rich aminosilicone solvent at one or more process locations between the absorber and the desorber, to lower the viscosity of the solvent and to lower the temperature required for the desorption reaction.
1. A method for separating carbon dioxide (CO2) from a gas stream, comprising:
feeding the gas stream to an absorber through which a lean aminosilicone solvent circulates;
reacting the gas stream with the lean aminosilicone solvent within the absorber at a first temperature range, so as to generate a rich aminosilicone solvent stream and a clean gas stream with reduced CO2 in comparison with the initial gas stream;
directing the rich aminosilicone solvent stream to a desorber that heat-treats the rich solvent in an endothermic desorption/regeneration reaction that is carried out at a second temperature range higher than the first temperature range; to regenerate lean aminosilicone solvent and to produce carbon dioxide gas;
directing the regenerated, lean aminosilicone solvent through a steam-producing, indirect heat exchanger configured to supply steam to the desorber and sustain the endothermic desorption reaction and to lower the partial pressure of CO2 in the vapor phase in the lower region of the desorber;
boiling an amount of steam in the indirect heat exchanger in excess of an amount that is required to provide the heat of reaction for aminosilicone desorption, so as to maintain steam in the vapor phase in the upper region of the desorber; and
adding selected amounts of make-up water from a make-up water stream to the rich aminosilicone solvent stream, at one or more process locations between an exit site for the absorber and an inlet site for the desorber, to lower the viscosity of the rich aminosilicone solvent and to lower the temperature required for the desorption reaction, wherein CO2 and entrained water vapor/steam released during the desorption reaction is directed to a condenser to separate CO2 from the entrained water vapor/steam, such that water separated in the condenser is fed to the desorber as at least one source of the make-up water.
2. The method of claim 1 , wherein the aminosilicone solvent is a liquid material, functionalized with one or more groups that reversibly react with CO2, and/or have a high affinity for CO2.
3. The method of claim 2 , wherein the aminosilicone solvent is functionalized with one or more nitrogen atom-containing groups.
4. The method of claim 3 , wherein the functional group comprises a primary or secondary aliphatic or aromatic amine, imine, amidine, a heterocyclic amino compound, or combinations thereof.
5. The method of claim 1 , wherein the aminosilicone solvent is in admixture with at least one hydroxy-containing solvent, to form a solvent system.
6. The method of claim 5 , wherein the hydroxy-containing solvent is a glycol.
7. The method of claim 5 , wherein the absorber is equipped with at least one device to cool the solvent system during the reaction with the gas stream.
8. The method of claim 1 , wherein the clean gas stream is directed to a water wash system that is also fed by at least one water source; and is configured to separate a stripped portion of the lean aminosilicone solvent from the clean gas stream, so as to generate a CO2-depleted exhaust gas and a mixture of the water and the stripped portion of the lean solvent.
9. The method of claim 8 , wherein at least a portion of the mixture of the water and the stripped portion of the lean solvent is directed to a water-wash storage tank that is capable of separating the water from the stripped portion of the solvent.
10. The method of claim 9 , wherein the stripped portion of the solvent is directed back to the absorber.
11. The method of claim 10 , wherein the stripped portion of the solvent being directed back to the absorber is directed to a lean solvent storage tank situated between the water-wash storage tank and the absorber.
12. The method of claim 1 , wherein the lean aminosilicone solvent passing through the steam-producing, indirect heat exchanger is directed back to the absorber.
13. The method of claim 12 , wherein the lean aminosilicone solvent being directed back to the absorber passes through at least one rich-lean heat exchanger situated between the absorber and the desorber, to reduce the temperature of the solvent to the first temperature range for the absorption reaction.
14. The method of claim 13 , wherein adding selected amounts of make-up water is carried out at a location between the absorber and the rich-lean heat exchanger or at a location between the rich-lean heat exchanger and the desorber.
15. The method of claim 13 , wherein adding selected amounts of make-up water is carried out at a location between the absorber and the rich-lean heat exchanger and also at a location between the rich-lean heat exchanger and the desorber.
16. The method of claim 13 , wherein the lean aminosilicone solvent being directed back to the absorber and passing through the rich-lean heat exchanger is directed through at least one additional cooling mechanism.
17. The method of claim 1 , wherein the amount (total) of additional make-up water is an amount sufficient to provide a steady state water content of the rich aminosilicone solvent stream between about 5 weight percent and about 25 weight percent.
18. The method of claim 1 , wherein the first temperature range for reaction of the fluid stream with the lean aminosilicone solvent within the absorber is from about 25° C. to about 80° C.
19. The method of claim 1 , wherein the second temperature range for the desorption/regeneration reaction is in the range of about 90° C. to about 140° C.
20. The method of claim 1 , wherein the amount of steam supplied to the desorber apparatus is sufficient to decrease the vapor pressure of CO2 in the desorber.
21. The method of claim 1 , wherein lean solvent includes at least one of oxidation inhibitors, anti-foaming agents, or corrosion inhibitors.
22. The method of claim 1 , further comprising
receiving the lean solvent at a purge-reclaim station located downstream from the indirect heat exchanger, and
filtering, via the purge-reclaim station, detached aminosilicone molecules from the lean solvent.
23. A method for separating carbon dioxide (CO2) from a gas stream, comprising:
reacting the gas stream with a lean aminosilicone solvent in an absorber, resulting in a rich aminosilicone solvent that is then treated in a desorber to release the CO2 and regenerate lean aminosilicone solvent in a desorption reaction;
directing the regenerated solvent into a steam-producing, indirect heat exchanger configured to supply steam to the desorber to augment the desorption reaction; and
adding selected amounts of make-up water to the rich aminosilicone solvent at one or more process locations between the absorber and the desorber, to lower the viscosity of the solvent and to lower the temperature required for the desorption reaction;
wherein CO2 and entrained water vapor/steam released during the desorption reaction is directed to a condenser to separate CO2 from the entrained water vapor/steam, such that water separated in the condenser is fed to the desorber as at least one source of the make-up water.