Simultaneous high efficiency capture of CO
Low-cost and energy-efficient CO 2 and H 2 S capture is provided obtaining greater than 99.9% capture efficiency from pressurized gas. The acid species are captured in an ammonia solution, which is then regenerated by stripping the absorbed species. The solution can capture as much as 330 grams of CO 2 and H 2 S per 1000 gram of water and when regenerated it produces pure pressurized acid gas containing more than 99.7% CO 2 and H2S. The absorption of the acid species is accomplished in two absorbers in-series, each having multiple stages. More than 95% of the acid species are captured in the first absorber and the balance is captured in the second absorber to below 10 ppm concentration in the outlet gas. The two absorbers operate at temperatures ranging from 20-70 degrees Celsius. The two absorbers and the main stripper of the alkaline solution operate at similar pressures ranging from 5-200 bara.
1. A system for a multi-staged capture of CO 2 and H 2 S from a pressurized gas stream producing a clean pressurized gas stream containing less than 1 ppm H 2 S and less than 10 ppm CO 2 and achieving greater than 99.9% capture efficiency, wherein the pressure in said pressurized gas stream and said clean pressurized gas stream is above atmospheric pressure, comprising:
(a) an alkaline solution containing 5-15 molal NH 3 ;
(b) a first multistage absorber for absorbing CO 2 and H 2 S from said pressurized gas stream combined with said alkaline solution, wherein greater than 95% of said CO 2 and H 2 S content of said pressurized gas stream is captured in said alkaline solution, wherein a net loading of 110-330 grams of said C0 2 and H 2 S per 1000 grams of water is absorbed in said alkaline solution;
(c) a second multistage polishing absorber using water for capturing the residual of CO 2 and H 2 S in said pressurized gas stream entrained from said first multistage absorber and NH 3 entrained from said first multistage absorber resulting in a gas outlet stream from said second multistage polishing absorber containing less than 10 ppm CO 2 and NH 3 and less than 1 ppm H 2 S;
(d) a main stripper for stripping said CO 2 and H 2 S absorbed by said first multistage absorber in said alkaline solution, resulting in:
(i) a pure gas stream exhausted containing greater than 99.7% CO 2 +H 2 S, less than 0.3% water vapor and less than 10 ppm of each of H 2 , CO, NH 3 and CH 4 , and
(ii) said alkaline solution reduced of said stripped CO 2 and H 2 S which is sent back from said main stripper to said first multistage absorber,
(e) a sour water stripper for stripping said CO 2 , H 2 S and NH 3 absorbed by said second multistage polishing absorber in said water, and said water stripped of said CO 2 , H 2 S and NH 3 is sent back from said sour water stripper to said second multistage polishing absorber.
2. The system as set forth in claim 1 , wherein said pressurized gas stream comprises an H 2 S concentration in the range of 0-7% mole and a CO 2 concentration in the range of 1-50% mole.
3. The system as set forth in claim 1 , wherein said alkaline solution further comprises alkaline cations, wherein said alkaline cations are Na + , K + , Li + , or a combination thereof.
4. The system as set forth in claim 1 , wherein the said pressurized gas stream is at a pressure in the range of 5-200 bara, wherein said first multistage absorber and said second multistage polishing absorber operate at a pressure in the range of 5-200 bara, and wherein said main stripper operates at a pressure in the range of 5-200 bara.
5. The system as set forth in claim 1 , wherein said first multistage absorber comprises at least two absorption stages, wherein each of said absorption stages is a gas-liquid contact vessel.
6. The system as set forth in claim 5 , wherein one of said at least two absorption stages comprises: (i) said alkaline solution having a NH 3 /CO 2 mole ratio in the range of 0.2-0.4, and (ii) an operating temperature in the range of 20-40 degrees Celsius.
7. The system as set forth in claim 5 , wherein one of said at least two absorption stages comprises: (i) said alkaline solution having a NH 3 /CO 2 mole ratio in the range of 0.3-0.55, and (ii) an operating temperature in the range of 35-60 degrees Celsius.
8. The system as set forth in claim 5 , wherein one of said at least two absorption stages comprises: (i) said alkaline solution having a NH 3 /CO 2 mole ratio in the range of 0.5-0.7, and (ii) an operating temperature in the range of 50-70 degrees Celsius.
9. The system as set forth in claim 1 , wherein said second multistage polishing absorber comprises at least two absorption stages to reduce CO 2 and H 2 S emission to ppm level concentrations.
10. The system as set forth in claim 9 , wherein one of said at least two absorption stages comprises: (i) a water-ammonia solution with an NH 3 concentration in the range of 0-0.2 molal, and (ii) a CO 2 /NH 3 mole ratio in said water of less than 0.5.
11. The system as set forth in claim 9 , wherein one of said at least two absorption stages comprises: (i) an NH 3 concentration in the range of 1-6 molal, and (ii) a CO 2 /NH 3 mole ratio in said water of less than 0.5.
12. The system as set forth in claim 1 , wherein said main stripper further comprises an integrated NH 3 washing stage.