Method for capturing CO2 with assisted vapor compression

Abstract

The present application provides processes and systems for direct capture of CO.sub.2 from an ambient air or a flue gas using large excess of steam and a vapor compression cycle.

Claims

1. A method of capturing CO.sub.2 from a CO.sub.2-enriched gaseous stream, the method comprising: (i) contacting the CO.sub.2-enriched gaseous stream with a CO.sub.2-depleted solid hydrophobic sorbent material at about ambient temperature and at about ambient pressure, to produce a CO.sub.2-depleted gaseous stream and a CO.sub.2-enriched solid hydrophobic sorbent material; (ii) contacting the CO.sub.2-enriched solid hydrophobic sorbent material produced in step (i) with a stream of steam at a first pressure and a first temperature, to produce the CO.sub.2-depleted solid hydrophobic sorbent material and a CO.sub.2-enriched stream of steam; wherein the first temperature is greater than the ambient temperature, and the first pressure is equal or below the saturation pressure corresponding to the first temperature; (iii) compressing the CO.sub.2-enriched stream of steam produced in step (ii) to a second pressure and a second temperature, to produce a hot compressed CO.sub.2-enriched stream of steam; wherein the second temperature is greater than the first temperature, and the second pressure is greater than the first pressure; (iv) condensing the hot compressed CO.sub.2-enriched stream of steam produced in step (iii) to produce a stream of gaseous CO.sub.2 at about a third temperature, a stream of water at about the first pressure and a fourth temperature, and an amount of thermal energy; wherein the second temperature is greater than the third temperature and the fourth temperature, and the first temperature is greater than or about equal to the fourth temperature; (v) heating the stream of water produced in step (iv) to produce the stream of steam at the first pressure and the first temperature for use in step (ii) using the thermal energy produced in step (iv); and (vi) contacting the CO.sub.2-enriched solid hydrophobic sorbent material produced in step (i) with the stream of gaseous CO.sub.2 produced in step (iv) to produce a stream of gaseous CO.sub.2 at a fifth temperature and the CO.sub.2-enriched solid hydrophobic sorbent material produced in step (i) at a temperature lower than or equal to the first temperature for use in step (ii); wherein the fifth temperature is lower than the third temperature.

2. The method of claim 1, wherein the CO.sub.2-enriched gaseous stream is ambient air.

3. The method of claim 2, wherein the ambient air comprises from about 200 ppm to about 1000 ppm of CO.sub.2.

4. The method of claim 1, wherein the CO.sub.2-enriched gaseous stream is flue gas.

5. The method of claim 4, wherein the flue gas comprises from about 3 vol. % to about 35 vol. % of CO.sub.2.

6. The method of claim 1, wherein the solid hydrophobic sorbent material is selected from an amine compound on a solid support, a zeolite, activated carbon, a metal-organic framework.

7. The method of claim 1, wherein the adsorption capacity of the CO.sub.2-depleted solid hydrophobic sorbent material is from about 5 mg CO.sub.2 to about 500 mg per about 1 g of the solid hydrophobic sorbent material.

8. The method of claim 1, wherein CO.sub.2 capture rate in step (i) is from about 50 wt. % to about 100 wt. % relative to the initial amount of CO.sub.2 in the CO.sub.2 enriched gaseous stream.

9. The method of claim 1, wherein the first pressure of the stream of steam in step (ii) is from about 0.5 bar to about 2 bar, and the first temperature of the stream of steam in step (ii) is from about 80° C. to about 200° C.

10. The method of claim 1, wherein molar ratio of water to CO.sub.2 in the CO.sub.2-enriched stream of steam produced in step (ii) is from about 50:1 to about 500:1.

11. The method of claim 1, wherein a ratio of the second pressure to the first pressure is from about 1.01:1 to about 100:1.

12. The method of claim 1, wherein: the second pressure is about 1.5 bar and the first pressure is about 1 bar, and the second temperature is about 145° C. and the first temperature is about 100° C.

13. The method of claim 1, wherein from about 50 wt. % to about 100 wt. % of steam is condensed during condensing the hot compressed CO.sub.2-enriched stream of steam in process (iv).

14. The method of claim 1, wherein the method is carried out in a batch mode or in a continuous mode.

15. A method of capturing CO.sub.2 from a CO.sub.2-enriched gaseous stream, the method comprising: contacting the CO.sub.2-enriched gaseous stream with a CO.sub.2-depleted solid water-adsorbing sorbent material at about ambient temperature and at about ambient pressure, to produce a CO.sub.2-depleted gaseous stream and a CO.sub.2-enriched solid water-adsorbing sorbent material; (ii) contacting the CO.sub.2-enriched solid water-adsorbing sorbent material produced in step (i) with a stream of steam at a first pressure and a first temperature, to produce the CO.sub.2-depleted solid water-adsorbing sorbent material and a CO.sub.2-enriched stream of steam; wherein the first temperature is greater than the ambient temperature, and the first pressure is equal or below the saturation pressure corresponding to the first temperature; (iii) compressing the CO.sub.2-enriched stream of steam produced in step (ii) to a second pressure and a second temperature, to produce a hot compressed CO.sub.2-enriched stream of steam; wherein the second temperature is greater than the first temperature, and the second pressure is greater than the first pressure; (iv) condensing the hot compressed CO.sub.2-enriched stream of steam produced in step (iii) to produce a stream of gaseous CO.sub.2 at about a third temperature, a stream of water at about the first pressure and a fourth temperature, and an amount of thermal energy; wherein the second temperature is greater than the third temperature and the fourth temperature, and the first temperature is greater than or about equal to the fourth temperature; (v) heating the stream of water produced in step (iv) to produce the stream of steam at the first pressure and the first temperature for use in step (ii) using the thermal energy produced in step (iv); and (vi) contacting the CO.sub.2-enriched solid water-adsorbing sorbent material produced in step (i) with the stream of gaseous CO.sub.2 produced in step (iv) to produce a stream of gaseous CO.sub.2 at a fifth temperature and the CO.sub.2-enriched solid water-adsorbing sorbent material produced in step (i) at a temperature lower than or equal to the first temperature for use in step (ii); wherein the fifth temperature is lower than the third temperature.

16. The method of claim 15, wherein the CO.sub.2-enriched gaseous stream is ambient air.

17. The method of claim 16, wherein the ambient air comprises from about 200 ppm to about 1000 ppm of CO.sub.2.

18. The method of claim 15, wherein the CO.sub.2-enriched gaseous stream is flue gas.

19. The method of claim 18, wherein the flue gas comprises from about 3 vol. % to about 35 vol. % of CO.sub.2.

20. The method of claim 15, wherein the adsorption capacity of the CO.sub.2-depleted solid water-adsorbing sorbent material is from about 5 mg CO.sub.2 to about 500 mg per about 1 g of the solid water-adsorbing sorbent material.

21. The method of claim 15, wherein CO.sub.2 capture rate in step (i) is from about 50 wt. % to about 100 wt. % relative to the initial amount of CO.sub.2 in the CO.sub.2 enriched gaseous stream.

22. The method of claim 15, wherein the first pressure of the stream of steam in step (ii) is from about 0.5 bar to about 2 bar, and the first temperature of the stream of steam in step (ii) is from about 80° C. to about 200° C.

23. The method of claim 15, wherein molar ratio of water to CO.sub.2 in the CO.sub.2-enriched stream of steam produced in step (ii) is from about 50:1 to about 500:1.

24. The method of claim 15, wherein a ratio of the second pressure to the first pressure is from about 1.01:1 to about 100:1.

25. The method of claim 15, wherein: the second pressure is about 1.5 bar and the first pressure is about 1 bar, and the second temperature is about 145° C. and the first temperature is about 100° C.

26. The method of claim 15, wherein from about 50 wt. % to about 100 wt. % of steam is condensed during condensing the hot compressed CO.sub.2-enriched stream of steam in process (iv).

27. The method of claim 15, wherein the method is carried out in a batch mode or in a continuous mode.

28. A method of capturing CO.sub.2 from a CO.sub.2-enriched gaseous stream, the method comprising: contacting the CO.sub.2-enriched gaseous stream with a CO.sub.2-depleted sorbent material at about ambient temperature and at about ambient pressure, to produce a CO.sub.2-depleted gaseous stream and a CO.sub.2-enriched sorbent material; (ii) contacting the CO.sub.2-enriched sorbent material produced in step (i) with a stream of steam at a first pressure and a first temperature, to produce the CO.sub.2-depleted sorbent material and a CO.sub.2-enriched stream of steam; wherein the first temperature is greater than the ambient temperature, and the first pressure is equal or below the saturation pressure corresponding to the first temperature; (iii) compressing the CO.sub.2-enriched stream of steam produced in step (ii) to a second pressure and a second temperature, to produce a hot compressed CO.sub.2-enriched stream of steam; wherein the second temperature is greater than the first temperature, and the second pressure is greater than the first pressure; (iv) condensing the hot compressed CO.sub.2-enriched stream of steam produced in step (iii) to produce a stream of gaseous CO.sub.2 at about a third temperature, an initially formed stream of water at the second pressure, and an amount of thermal energy; (v) decompressing the initially formed stream of water at the second pressured in step (iv) to form a stream of water at about the first pressure and the fourth temperature; wherein the second temperature is greater than the third temperature and the fourth temperature, and the first temperature is greater than or about equal to the fourth temperature; (vi) heating the stream of water produced in step (v) to produce the stream of steam at the first pressure and the first temperature for use in step (ii) using the thermal energy produced in step (iv); and (vii) contacting the CO.sub.2-enriched sorbent material produced in step (i) with the stream of gaseous CO.sub.2 produced in step (iv) to produce a stream of gaseous CO.sub.2 at a fifth temperature and the CO.sub.2-enriched sorbent material produced in step (i) at a temperature lower than or equal to the first temperature for use in step (ii); wherein the fifth temperature is lower than the third temperature.

29. The method of claim 28, wherein the CO.sub.2-enriched gaseous stream is ambient air.

30. The method of claim 29, wherein the ambient air comprises from about 200 ppm to about 1000 ppm of CO.sub.2.

31. The method of claim 28, wherein the CO.sub.2-enriched gaseous stream is flue gas.

32. The method of claim 31, wherein the flue gas comprises from about 3 vol. % to about 35 vol. % of CO.sub.2.

33. The method of claim 28, wherein the adsorption capacity of the CO.sub.2-depleted sorbent material is from about 5 mg CO.sub.2 to about 500 mg per about 1 g of sorbent material.

34. The method of claim 28, wherein CO.sub.2 capture rate in step (i) is from about 50 wt. % to about 100 wt. % relative to the initial amount of CO.sub.2 in the CO.sub.2 enriched gaseous stream.

35. The method of claim 28, wherein the first pressure of the stream of steam in step (ii) is from about 0.5 bar to about 2 bar, and the first temperature of the stream of steam in step (ii) is from about 80° C. to about 200° C.

36. The method of claim 28, wherein molar ratio of water to CO.sub.2 in the CO.sub.2-enriched stream of steam produced in step (ii) is from about 50:1 to about 500:1.

37. The method of claim 28, wherein a ratio of the second pressure to the first pressure is from about 1.01:1 to about 100:1.

38. The method of claim 28, wherein: the second pressure is about 1.5 bar and the first pressure is about 1 bar, and the second temperature is about 145° C. and the first temperature is about 100° C.

39. The method of claim 28, wherein from about 50 wt. % to about 100 wt. % of steam is condensed during condensing the hot compressed CO.sub.2-enriched stream of steam in process (iv).

40. The method of claim 28, comprising using the stream of liquid water at the fifth temperature to cool the CO.sub.2-depleted sorbent material produced in step (ii) from about the first temperature to about the fifth temperature.

41. The method of claim 28, wherein the method is carried out in a batch mode or in a continuous mode.

42. A method of capturing CO.sub.2 from a CO.sub.2-enriched gaseous stream, the method comprising: (i) contacting the CO.sub.2-enriched gaseous stream with a CO.sub.2-depleted sorbent material at about ambient temperature and at about ambient pressure, to produce a CO.sub.2-depleted gaseous stream and a CO.sub.2-enriched sorbent material; (ii) contacting the CO.sub.2-enriched sorbent material produced in step (i) with a stream of steam at a first pressure and a first temperature, to produce the CO.sub.2-depleted sorbent material and a CO.sub.2-enriched stream of steam; wherein the first temperature is greater than the ambient temperature, and the first pressure is equal or below the saturation pressure corresponding to the first temperature; (iii) compressing the CO.sub.2-enriched stream of steam produced in step (ii) to a second pressure and a second temperature, to produce a hot compressed CO.sub.2-enriched stream of steam; wherein the second temperature is greater than the first temperature, and the second pressure is greater than the first pressure; (iv) condensing the hot compressed CO.sub.2-enriched stream of steam produced in step (iii) to produce a stream of gaseous CO.sub.2 at about a third temperature, a stream of water at about the first pressure and a fourth temperature, and an amount of thermal energy; wherein the second temperature is greater than the third temperature and the fourth temperature, and the first temperature is greater than or about equal to the fourth temperature; (v) heating the stream of water produced in step (iv) to produce the stream of steam at the first pressure and the first temperature for use in step (ii) using the thermal energy produced in step (iv); (vi) contacting the CO.sub.2-enriched sorbent material produced in step (i) with the stream of gaseous CO.sub.2 produced in step (iv) to produce a stream of gaseous CO.sub.2 at a fifth temperature and the CO.sub.2-enriched sorbent material produced in step (i) at a temperature lower than or equal to the first temperature for use in step (ii); wherein the fifth temperature is lower than the third temperature; and (vii) using a stream of liquid water at the fifth temperature to cool the CO.sub.2-depleted sorbent material produced in step (ii) from about the first temperature to about the fifth temperature.

43. The method of claim 42, wherein the CO.sub.2-enriched gaseous stream is ambient air.

44. The method of claim 43, wherein the ambient air comprises from about 200 ppm to about 1000 ppm of CO.sub.2.

45. The method of claim 42, wherein the CO.sub.2-enriched gaseous stream is flue gas.

46. The method of claim 45, wherein the flue gas comprises from about 3 vol. % to about 35 vol. % of CO.sub.2.

47. The method of claim 42, wherein the adsorption capacity of the CO.sub.2-depleted sorbent material is from about 5 mg CO.sub.2 to about 500 mg per about 1 g of sorbent material.

48. The method of claim 42, wherein CO.sub.2 capture rate in step (i) is from about 50 wt. % to about 100 wt. % relative to the initial amount of CO.sub.2 in the CO.sub.2 enriched gaseous stream.

49. The method of claim 42, wherein the first pressure of the stream of steam in step (ii) is from about 0.5 bar to about 2 bar, and the first temperature of the stream of steam in step (ii) is from about 80° C. to about 200° C.

50. The method of claim 42, wherein molar ratio of water to CO.sub.2 in the CO.sub.2-enriched stream of steam produced in step (ii) is from about 50:1 to about 500:1.

51. The method of claim 42, wherein a ratio of the second pressure to the first pressure is from about 1.01:1 to about 100:1.

52. The method of claim 42, wherein: the second pressure is about 1.5 bar and the first pressure is about 1 bar, and the second temperature is about 145° C. and the first temperature is about 100° C.

53. The method of claim 42, wherein from about 50 wt. % to about 100 wt. % of steam is condensed during condensing the hot compressed CO.sub.2-enriched stream of steam in process (iv).

54. The method of claim 42, wherein the method is carried out in a batch mode or in a continuous mode.

Description

DESCRIPTION OF DRAWINGS

(1) FIG. 1 is a schematic diagram of an exemplary process of the present disclosure.

(2) FIG. 2 is a flow chart detailing an exemplary process of the present disclosure.

DETAILED DESCRIPTION

(3) In one general aspect, the present disclosure provides an adsorption-based CO.sub.2 capture process. Generally, in such a process, the sorbent goes through four distinct phases. In phase I, a sorbent material is used to capture CO.sub.2 from a CO.sub.2-enriched gaseous stream, such as ambient air or flue gas. In phase II, the CO.sub.2-enriched sorbent material is heated to reach the CO.sub.2 desorption conditions. Then, in phase III, the material is heated to desorb CO.sub.2 and regenerate the sorbent material. The phase III process may be carried out by blowing steam through the bed of the CO.sub.2-enriched sorbent. The steam provides sufficient heat for the desorption to take place, and also serves as a sweeping force to carry CO.sub.2 away from the surface of the sorbent material. In this phase, after all or nearly all of the CO.sub.2 is desorbed, steam may be condensed to liquid water, and the liquid water separated from gaseous CO.sub.2, for example, in a phase separator. Finally, in phase IV, the regenerated sorbent is cooled to its initial temperature, to be reused in phase I of the same process.

(4) Conventionally, all four phases of such a process required a large amount of thermal energy, for example, to generate steam and to heat the CO.sub.2-enriched sorbent to the required temperature for desorption. That thermal energy is usually lost with the waste water resulting from condensation of the steam to separate the concentrated CO.sub.2 gas.

(5) The methods and systems of the present disclosure advantageously allow to recover heat lost during cooling of regenerated sorbent in phase IV and use that heat to warm up the CO.sub.2-enriched sorbent in phase II. These methods and systems also allow to recover heat from steam condensation and use that heat to evaporate liquid water to produce hot steam for use in the desorption process of phase III.

(6) In some embodiments, the present disclosure provides a method of capturing CO.sub.2 from a CO.sub.2-enriched gaseous stream. An exemplary process 200 within the present claims is schematically shown on FIG. 2. Referring to FIG. 2, the process 200 includes step 202 of contacting the CO.sub.2-enriched gaseous stream with a CO.sub.2-depleted sorbent material at about ambient temperature (T.sup.atm) and at about ambient pressure (P.sup.atm), to produce a CO.sub.2-depleted gaseous stream and a CO.sub.2-enriched sorbent material. Step 204 of the process includes contacting the CO.sub.2-enriched sorbent material produced in step 202 with a stream of steam at a first pressure (P.sup.1) and a first temperature (T.sup.1), to produce the CO.sub.2-depleted sorbent material and a CO.sub.2-enriched stream of steam. In some embodiments, the T.sup.1 is greater than the T.sup.atm, and the P.sup.1 is equal or below the saturation pressure corresponding to T.sup.1. Step 204 of the process 200 is followed by step 206, which includes compressing the CO.sub.2-enriched stream of steam produced in step 204 to a second pressure (P.sup.2) and a second temperature (T.sup.2), to produce a hot compressed CO.sub.2-enriched stream of steam. In some embodiments, the T.sup.2 is greater than the T.sup.1, and the P.sup.2 is greater than the P.sup.1. Step 208 of the process 200 includes condensing the hot compressed CO.sub.2-enriched stream of steam produced in step 206 to produce a stream of gaseous CO.sub.2 at about a third temperature (T.sup.3), a stream of water at about the P.sup.1 and a fourth temperature (T.sup.4), and an amount of a thermal energy. In some embodiments of the process 200, the T.sup.2 is greater than the T.sup.3 and the T.sup.4, and the T.sup.1 is greater than or about equal to the T.sup.4. The process 200 further includes a step 210 of heating the stream of water produced in step 208 to produce the stream of steam at the P.sup.1 and the T.sup.1 for use in step 204, using the thermal energy produced in step 208. Finally, the process 200 also includes the step 212 of contacting the CO.sub.2-enriched sorbent material produced in step 202 with the stream of gaseous CO.sub.2 produced in step 208 to produce a stream of gaseous CO.sub.2 at a T.sup.5 and the CO.sub.2-enriched sorbent material produced in step 202 at a temperature lower than or equal to the T.sup.1 for use in step 204. In some embodiments, the T.sup.5 is lower than the T.sup.3.

(7) In some embodiments, the process 200 may also include a step 214 which includes using the stream of liquid water at the T.sup.5 to cool the CO.sub.2-depleted sorbent material produced in step 204 from about the T.sup.1 to about the T.sup.5. In this process, the liquid water may be warmed up from the T.sup.5 to a temperature lower than or about equal to the T.sup.1.

(8) In some embodiments, the process 200 may also include a step 214 which includes using the stream of gaseous CO.sub.2 at the T.sup.5 to cool the CO.sub.2-depleted sorbent material produced in step 204 from about the T.sup.1 to about the T.sup.atm (or T.sup.5). In this process, the pure gaseous CO.sub.2 may be warmed up from the T.sup.5 to a temperature lower than or about equal to the T.sup.1.

(9) Certain embodiments of this process are described herein. As used throughout this disclosure, the term “about” means “approximately” (e.g., plus or minus approximately 10% of the indicated value).

(10) The CO.sub.2-enriched gaseous stream maybe any gas or a mixture of gases containing a removable amount of CO.sub.2. One example of such a stream is air. Generally, ambient atmospheric air contains from about 200 to about 1000 ppm of CO.sub.2. In some embodiments, the ambient air useful in the processes of this disclosure contains CO.sub.2 in an amount of about 250 ppm, about 300 ppm, about 350 ppm, about 400 ppm, or about 1000 ppm. The air typically contains other gases besides CO.sub.2, for example, the air may contain from about 20 v. % to about 22 v. % of O.sub.2, from about 77 v. % to about 79 v. % of N.sub.2, from about 0.5 v. % to about 1 v. % of Ar, as well as minor amounts of H.sub.2O, CO, CH.sub.4, and other gases. Another example of the CO.sub.2-enriched stream is a flue gas. Such a flue gas may contain from about 3 v. % to about 35 v. % of CO.sub.2, as well as H.sub.2O, NO.sub.2, SO.sub.2, and the other gases that the air contains or that are produced during burning of fossil fuels. For example, CO.sub.2-enriched gaseous stream may contain about 1 v. %, about 2 v. %, about 5 v. %, about 10 v. %, about 15 v. %, about 20 v. %, or about 25 v. % of CO.sub.2.

(11) The CO.sub.2-depleted sorbent material may be any material that is substantially free of CO.sub.2 and that has the capacity and ability to selectively adsorb CO.sub.2 on its surface when that surface is brought in contact with a gaseous stream containing the CO.sub.2. Examples of sorbent material include solid sorbents and liquid based sorbents. Examples of liquid based sorbents include various liquids incorporating solid sorbents by means of suspension or encapsulation for example. Suitable examples of solid sorbents include amine compounds on a solid support, zeolites, activated carbon, metal-organic frameworks. In some embodiments, the solid sorbent is a chemisorbent, selectively and reversibly chemically reacting with CO.sub.2, forming a new chemical compound such as an organic amide or a carbamate, or organic and inorganic carbonates. In other embodiments, the solid sorbent is a physisorbent that adsorbs CO.sub.2 non-covalently, for example, by forming H-bonding, hydrophobic interaction, electrostatic interactions, or Van der Waals forces between the surface of the adsorbent and the molecules of CO.sub.2. The physisorbents are typically materials with high porosity having a very large surface area, allowing for physical reversible adhesion of a large amount of molecules of CO.sub.2 on the surface.

(12) In some embodiments, the solid sorbent material is hydrophobic. In one example, the contact angle of a water drop on the surface of the solid sorbent is greater than about 90 deg, about 100 deg, about 120 deg, or about 150 deg. In these embodiments, the sorbent material in tower 114 (referring to FIG. 1) in phase IV of the process is substantially free from water. Any water that remained after sweep steaming the CO.sub.2-enriched adsorbent drips down from the sorbent bed, leaving behind substantially dry material. In other embodiments, the sorbent material is prone to water capture, having an ability to adsorb a substantial amount of water. In one example, the water adsorbing sorbent may adsorb about 5 wt. %, about 10 wt. %, about 15 wt. %, or about 20 wt. % of water relative to the weight of the dry sorbent material.

(13) In some embodiments, the CO.sub.2-depleted sorbent material in step 202 of the process 200 has the ability to adsorb from about 5 mg CO.sub.2 to about 500 mg per about 1 g of sorbent material. In one example, the adsorption capacity of the sorbent material is about 40 mg, about 60 mg, about 80 mg, about 100 mg, or about 200 mg of CO.sub.2 per about 1 g of the sorbent material.

(14) To contact the depleted sorbent with the stream containing CO.sub.2 in the step 202 of the process 200, the stream can be blown through a single tower or a plurality of towers. A tower containing sorbent beds may be constructed such that the air/gas flow rate is from about 1 m.sup.3/hour to about 100,000 m.sup.3/hour, for example, about 100 m.sup.3/hour, about 1000 m.sup.3/hour, about 10,000 m.sup.3/hour, about 20,000 m.sup.3/hour, about 30,000 m.sup.3/hour, or about 50,000 m.sup.3/hour.

(15) The step 202 of the process 200 may be carried out such that the capture rate of CO.sub.2 from the enriched stream is from about 1% to about 100%. For example, the capture rate may be from about 40% to about 100%, from about 50% to about 99%, from about 60% to about 95%, or from about 85% to about 95% of the total amount of CO.sub.2 in the enriched stream (e.g., air). In some embodiments, the capture rate is about 50%, about 60%, about 85%, about 95%, or about 99%. In one example, CO.sub.2 depleted stream exiting the step 202 contains the initial amount CO.sub.2 less the captured CO.sub.2. In this example, an amount of CO.sub.2 in the depleted stream is from about 1% to about 50%, from about 1% to about 25%, or from about 1% to about 10% of the initial amount of CO.sub.2 in the enriched stream entering the process 200. In some embodiments, the depleted stream is substantially free from CO.sub.2.

(16) In some embodiments, the CO.sub.2 enriched sorbent material generated in the step 202 of the process 200 contains about 10×, about 100×, about 1,000×, about 10,000×, or about 100,000× the amount of CO.sub.2 initially contained in the CO.sub.2 depleted sorbent material entering the process. In one example, the CO.sub.2 enriched sorbent material is saturated with CO.sub.2. That is, the sorbent material comprises from about 5 mg CO.sub.2 to about 500 mg per about 1 g of sorbent material (e.g., as described above). In some embodiments, the CO.sub.2 enriched sorbent material comprises from about 5 wt. % to about 25 wt. % of CO.sub.2 relative to the weight of the initial CO.sub.2 depleted material.

(17) In some embodiments, the step 202 of the process 200 is carried out at about T.sup.atm. That is, the CO.sub.2-enriched gaseous stream, such as air, is at about ambient temperature, and the CO.sub.2-depleted sorbent material is at about ambient temperature during the contacting. An example of ambient temperature is a temperature from about −15° C. to about 60° C., such as about 15° C., about 20° C., about 25° C., or about 35° C.

(18) In some embodiments, the step 202 of the process 200 is carried out at about P.sup.atm. That is, the gaseous stream and the sorbent material during the contacting are handled at about normal atmospheric pressure. An example of ambient pressure is a pressure from about 0.7 bar to about 1.5 bar, such as about 0.95 bar, about 0.99 bar, about 1 bar, about 1.01 bar, about 1.02 bar, about 1.05 bar, and about 1.1 bar.

(19) In order to desorb CO.sub.2 from the enriched (or saturated) sorbent, such sorbent may be contacted with steam in step 204 of the process 200. The steam may be blown into a tower containing the CO.sub.2-enriched sorbent at a pressure and temperature, and in an amount that is necessary for efficient desorption of CO.sub.2 from the sorbent. In some embodiments, the steam is blown to a tower containing a bed or beds of enriched sorbent at a P.sup.1 and a T.sup.1. In some embodiments, the T.sup.1 is greater than T.sup.atm. In some embodiments, the P.sup.1 is equal or below the saturation pressure corresponding to T.sup.1. The steam may be saturated or superheated. When blown into the tower, it comes in direct contact with the sorbent material. Generally, the sorbent material prior to this process is warmed up to about T.sup.1 during phase II of the process. The steam may also supply the heat necessary for desorption of CO.sub.2 and may sweep CO.sub.2 from the sorbent material.

(20) In some embodiments, because the sorbent bed is brought to T.sup.1 prior to steaming process, there is substantially no or minimal steam condensation in the adsorbent tower. The sorbent bed remains at T.sup.1 throughout the process and even after the steaming operation has ended. Because T.sup.1 is at or above the boiling point of water at P.sup.1, no condensation occurs. In the case of hydrophobic sorbent material, the de minimis amount of condensed water is repelled by the material and flows freely out of the tower. In the case of water adsorbing material, the de minimis amount of condensed water is absorbed by the sorbent material, which becomes dry and water-free during the cooling operation in phase IV.

(21) In some embodiments, the molar ratio of steam to CO.sub.2 during the desorption process is from about 50:1 to about 500:1. In one example, the molar ratio of steam to CO.sub.2 in the process is about 50:1, about 100:1, about 200:1, about 250:1, about 300:1, or about 400:1. The temperature of the sweeping steam (T.sup.1) may be from about 80° C. to about 500° C., and the absolute pressure of the steam (P.sup.1) may be from about 0.5 bar to about 40 bar. For example, the temperature T.sup.1 of the steam is from about 100° C. to about 200° C., and the absolute pressure P.sup.1 is from about 1 bar to about 2 bar. In some embodiments, the T.sup.1 is about 100° C., about 110° C., about 120° C., about 130° C., about 135° C., about 140° C., about 145° C., about 150° C., about 155° C., or about 160° C. In some embodiments, the P.sup.1 is about 0.7 bar, about 0.8 bar, about 0.9 bar, about 1 bar, about 1.1 bar, about 1.2 bar, about 1.5 bar, about 2 bar, about 5 bar, about 10 bar, or about 50 bar. In one example, P.sup.1 is substantially equal to P.sup.atm.

(22) The CO.sub.2-enriched stream of steam exits the step 204 to enter a compressor in step 206 of the process 200. In some embodiments, molar ratio of water vapor to CO.sub.2 in the CO.sub.2-enriched steam entering the compressor is from about 10:1 to about 2,000:1, from about 10:1 to about 1,500:1, from about 10:1 to about 1,000:1, from about 50:1 to about 400:1, or from about 50:1 to about 500:1. In some embodiments, the molar ratio is about 50:1, about 100:1, about 150:1, about 200:1, about 250:1, about 300:1, about 400:1, or about 500:1. The CO.sub.2-enriched steam exits the step 204 at about T.sup.1 and at about P.sup.1, and having the remaining physical characteristics similar to those of the sweeping steam. The compressor in the step 206 compresses the CO.sub.2-enriched steam to a pressure P.sup.2 that is greater than the pressure P.sup.1. In some embodiments, the pressure ratio in across the compressor (P.sup.2/P.sup.1) is from about 1.01:1 to about 100:1, from about 1.05:1 to about 50:1, from about 1.1:1 to about 40:1, from about 1.2:1 to about 30:1, or from about 1.01:1 to about 20:1. As a consequence of the increased pressure, temperature of the steam mixture also rises from T.sup.1 to T.sup.2. In one example, when pressure P.sup.2 is 1.2 bar (raised from P.sup.1 pressure of 1 bar), T.sup.2 raises to 120° C. (from T.sup.1 of 100° C.). In some embodiments, P.sup.2 is about 50 bar, about 40 bar, about 30 bar, about 20 bar, about 10 bar, about 5 bar, about 4 bar, about 3 bar, or about 2 bar. In some embodiments, T.sup.2 is 110° C., about 120° C., about 130° C., about 135° C., about 140° C., about 150° C., about 175° C., about 200° C., about 220° C., about 250° C., about 300° C., about 400° C., or about 500° C. The compressor used to create the compressed CO.sub.2-steam mixture at the pressure P.sup.2 is any one of the compressors known to one of ordinary skill in the art for such purpose. For example, the compressor, such as compressor 118 (referring to FIG. 1) may be a centrifugal compressor, a diaphragm compressor, or an axial compressor, each of which may have one stage or multiple stages depending on compression ratio. In the case of a multistage compressor, intercoolers can be used to increase the compression efficiency.

(23) The hot compressed CO.sub.2-enriched stream of steam created in step 206 may then be condensed in step 208, for example, by contacting the stream with a colder surface of a heat exchanger to condense the gaseous steam to a liquid water. Thus, the steam on the hot side of the heat exchanger is converted to a stream containing a gaseous phase consisting mainly of CO.sub.2 and a liquid water phase. In some embodiments, from about 50% to about 100% of steam is condensed in this process. In some embodiments, about 50%, about 60%, about 75%, about 80%, about 85%, about 90%, about 95%, about 99%, or about 100% of steam of the hot compressed mixture stream is condensed into liquid water in step 208. The liquid water produced in this process can have a pressure of about P.sup.1 and a temperature of about T.sup.4 that is lower than the T.sup.2 of the condensing steam. In some embodiments, the liquid water produced in the process can have a pressure of about P.sup.2 (which is subsequently expanded to P.sup.1) and temperature of about T.sup.4 that is lower than or about equal to the T.sup.2 of the condensing stream. The gaseous phase produced in step 208 on the hot side of the heat exchanger consists mainly of desorbed CO.sub.2 and any gaseous steam that was not converted to liquid water during the heat exchange and condensation of step 208. When the steam is condensing on the hot side on the exchanger, an amount of thermal energy (heat) is also produced. This heat is effectively transferred to the cooling liquid on the cold side of the heat exchanger, for example, during step 210 of the process 200.

(24) The gas/liquid mixture form the hot side of the heat exchanger in the step 208 may then be transferred to a phase separator, where the stream of gaseous CO.sub.2 at the pressure P.sup.2 and temperature T.sup.3 is separated from liquid water phase at pressure P.sup.2 and temperature T.sup.4. In some embodiments, T.sup.2 is greater than T.sup.3 and T.sup.4. In some embodiments, T.sup.3 is about equal to T.sup.4. In some embodiments, T.sup.3 is greater than T.sup.4.

(25) The liquid water produced in step 208 can then undergo decompression in an expansion device. Suitable examples of the expansion device include a throttling valve, a fixed orifice, and a turbine. The water is decompressed in this manner to the pressure P.sup.1 (while remaining at or about the temperature T.sup.4). In some embodiments, the pressure ratio (P.sup.1/P.sup.2) across the expansion device is the reverse of the pressure ratio formed in the compressor in step 206. For example, the pressure ratio across the expansion device (P.sup.2/P.sup.1) is from about 1.01:1 to about 100:1, from about 1.05:1 to about 50:1, from about 1.1:1 to about 40:1, from about 1.2:1 to about 30:1, or from about 1.01:1 to about 20:1.

(26) In step 210, the decompressed liquid water produced in step 208 can be recycled and re-used in the same step 208 by serving as a cooling liquid for condensing the hot compressed steam. For example, the stream of water can be supplied to the cool side of the heat exchanger in step 208, where the water is evaporated and converted into steam at about pressure P.sup.1 and at about temperature T.sup.1. Stream of steam produced in this manner can then be used in phase III (step 204) of the process 200. Effectively, the same heat exchanger can be used in both steps 208 and 210. This heat exchanger generally has two sides (hot and cold) with two different pressures: the hot P.sup.2 side where CO.sub.2-enriched steam supplied at T.sup.2 is condensing, and the cold P.sup.1 side where liquid water at P.sup.1 and about T.sup.4 (e.g., liquid water produced in step 208) is being evaporated to produce the steam at P.sup.1 and T.sup.1, to be used for CO.sub.2 desorption in step 204. In some embodiments, additional energy is needed to produce the required steam at P.sup.1 and T.sup.1; in such embodiments the additional energy can be brought by an external source of energy such as electrical heating, fuel combustion, geothermal energy or any other means of heating known to the person skilled in the art. The Δ(P.sup.2−P.sup.1) in this process can be set up in such a manner that the P.sup.2/T.sup.2 hot stream condensing temperature is from about 1° C. to about 50° C. higher than the P.sup.1/T.sup.1 liquid water evaporating temperature. In one example, the Δ(T.sup.2−T.sup.1) is from about 1° C. to about 40° C., from about 5° C. to about 50° C., from about 10° C. to about 50° C., or from about 20° C. to about 40° C. The pressurized steam condenses at higher temperature compared to the temperature of the evaporating liquid water, which enables direct heat transfer between the condensing steam and the evaporating fluid. Effectively, the entire amount of thermal energy (heat) produced during steam condensation is use to evaporate the same water that is formed during steam condensation.

(27) The gaseous CO.sub.2 stream is produced during phase separation in step 208 at the pressure P.sup.2 and a temperature T.sup.3 that is lower than or about equal to the temperature T.sup.2 of the condensing steam. The heat of this stream can be used in step 212 for heating the tower containing CO.sub.2-enriched sorbent material in phase II from T.sup.atm to a temperature between T.sup.atm and T.sup.1 to prepare the sorbent for the sweeping steam desorption phase III. This may be accomplished by contacting the enriched sorbent material (kept at T.sup.atm) with the gaseous CO.sub.2 stream (having temperature T.sup.3). The contacting may be carried out by the means of a heat exchanger, having CO.sub.2 stream on the hot side and the enriched sorbent on the cold side. After exiting this heat exchanger, the gaseous CO.sub.2 stream generally has a temperature T.sup.5 that is lower than the T.sup.3. For example, the temperature T.sup.3 may be 125° C., while temperature T.sup.5 may be from about 15° C. to about 50° C. In one example, the T.sup.5 is about equal to T.sup.atm. In another example, T.sup.5 is slightly higher than T.sup.atm.

(28) The process 200 may also include a step 214, where the liquid water at T.sup.5 can be used to cool the tower of regenerated sorbent in phase IV. In one embodiment, a CO.sub.2 stream produced at T.sup.5 can be used to cool the tower of regenerated sorbent in phase IV.

(29) In one aspect, the process 200 may also include a step 216 (not shown) for when the CO.sub.2 stream produced in step 208 after phase separation contains some steam (e.g., from about 5 wt. % to about 15 wt. % of steam, with the remainder being primarily CO.sub.2), that steam is generally condensed to liquid water when the stream is used to warm up the CO.sub.2 enriched sorbent in step 212. The gas/liquid stream exiting the now warmed up phase II tower at P.sup.2 and at or about T.sup.5 can be further cooled in a heat exchanger to T.sup.atm by using ambient air or a local water source. The gaseous CO.sub.2 phase can then be separated from the cold liquid water in a phase separator, and the cold liquid can be used to cool the phase IV CO.sub.2-depleted tower of step 204. The warm water that exits the tower at T.sup.6, that is generally lower than T.sup.4, can be depressurized (or decompressed) to P.sup.1 using an expansion device similar to that described above, and mixed with the stream of liquid water at P.sup.1 and T.sup.4 that was produced in step 208 after condensation of steam and phase separation. The mixed water streams are then used on the cold side of the heat exchanger in step 210 to produce steam for phase III (step 210), as described above.

(30) In some embodiments, the process of the present disclosure (e.g., the process 200 referring to FIG. 2 or the process 100 referring to FIG. 1) may be carried out in a batch mode. In other embodiments, the process may be carried out in a continuous mode. In a batch mode, multiple towers (or chambers) are used and the various streams, including the air stream, are directed to the various chambers sequentially for CO.sub.2 capture. The chamber can be isolated from any or all streams in order for an engineer to undertake the various steps required to regenerate the sorbent or cool it down to the initial state to start a new cycle. Another way to operate a batch process may be to move the solid sorbent without altering any of the stream pathways. In this manner, the sorbent, either enriched in CO.sub.2 or regenerated, is move from one chamber (or tower) to another to undergo the desorption/regeneration and the other steps. The process may be operated in a continuous manner using fluidized beds and sealing loops. A skilled engineer would be able to select and implement the appropriate machinery. Regardless of the mode of operation (batch or continuous), the process necessarily involves the four phases as discussed above.

(31) Exemplary Process and System for CO.sub.2 Capture

(32) An exemplary process 100 within the instant claims is schematically shown in FIG. 1. Referring to FIG. 1, a CO.sub.2-containing stream of air 102 is blown into a sorbent tower 104, wherein the CO.sub.2 is captured from the stream of air on or in the adsorbent material within the tower 104 (phase I of the process 100). In one example, the tower 104 is operated at ambient temperature and atmospheric pressure. A lean stream of air 106 exiting the adsorbent tower 104 is significantly depleted in CO.sub.2 as compared to the CO.sub.2 concentration in the stream 102. In one example, the lean stream 106 contains no more than about 10 ppm of CO.sub.2, or even no CO.sub.2 at all. A skilled mechanical engineer would be able to select and implement the process conditions (such as flow of air 102, an amount and kind of the adsorbent material, and dimensions of tower 104) to achieve this advantageous result. Once the sorbent material in the tower 104 is saturated with CO.sub.2 or has reached a pre-determined level of CO.sub.2 adsorption, the sorbent material is heated, for example, in tower 108 in order to bring the material to or near the regeneration temperature (phase II of the process 100). Once the material is heated to regeneration temperature in tower 108, the CO.sub.2 is desorbed from the material, for example, in tower 110, by blowing a heated steam 112 (hot water vapor) into the tower 110, until all or substantially all of the CO.sub.2 is removed by water vapor from the adsorbent material (phase III of the process 100). After that, the hot regenerated adsorbent material, depleted of CO.sub.2, is cooled to ambient temperature, for example, in tower 114 (phase IV of the process), in order to be recycled and reused in tower 104 in phase I of the process 100.

(33) During desorption of CO.sub.2 in phase III of the process 100, steam 112 exchanges heat with the sorbent material, thereby facilitating dissociation of CO.sub.2 from the material. In one example, temperature of the steam 112 is from about 80° C. to about 500° C., and the absolute pressure of the steam 112 is from about 0.5 bar to about 40 bar. In this example, the temperature of the steam 112 can be from about 100° C. to about 200° C., and the absolute pressure may be from about 1 bar to about 2 bar. The steam 112 also provides a sweeping force to carry the desorbed CO.sub.2 from the tower 110, and to form a gaseous mixture 116 consisting of steam and desorbed CO.sub.2, which then leaves the tower 110 for further processing. In one example, the weight ratio of steam to CO.sub.2 in the mixture 116 is from about 10:1 to about 2,000:1, such as from about 50:1 to about 400:1. After flowing out of the tower 110, the stream 116 is compressed in a compression device 118 to a pressure ratio from about 1:1.01 to about 1:20, to form a stream of a compressed hot gas 120. In one example, compressor 118 compresses the hot gas 116 to a pressure ratio from about 1:1.05 to about 1:2, thereby increasing the temperature of the compressed gas 120. In this example, when the pressure of stream 116 is 1 bar, and the compressor 118 increases the pressure ratio about 1.2:1, the resultant absolute pressure of the gas mixture 120 is about 1.2 bar and the temperature of the compressed H.sub.2O/CO.sub.2 gaseous stream 120 is from about 115° C. to about 145° C. The hot compressed gas 120 then enters a heat exchanger 122, where it is contacted with a colder surface and a large portion of the steam is therefore condensed to liquid water. In one example, from about 50 wt. % to about 100 wt. %, or from about 85 wt. % to about 99 wt. % of gaseous steam is condensed to form liquid water. The mixture 124 composed of liquid water, residual steam (if any), and desorbed gaseous CO.sub.2, while still under pressure, enters a phase separator device 126, where the liquid water 128 is physically separated from a gaseous phase 130. The liquid water 128 exits the separator 126 and enters an expansion device 132, to form a liquid water under a pressure equal to or slightly higher to that of the steam/CO.sub.2 mixture 116. In one example, the pressure ratio across the expansion device 132 is a reverse of the ratio for the compression device 118. In this example, the pressure ratio in 132 is from about 1.01:1 to about 20:1, or from about 1.05:1 to about 2:1.

(34) The vapor stream 130 leaving the separator 126 consists mainly of desorbed CO.sub.2 and uncondensed water vapor, if any. The stream 130 may also contain non-condensable gases that were adsorbed in tower 104 during phase I and desorbed in tower 110 during phase III. Suitable examples of those non-condensable gases include O.sub.2, N.sub.2, CH.sub.4, and Ar. The vapor stream 130 enters the tower 108 to exchange heat with the sorbent material in the tower during the heating phase II. This may be accomplished by using a heat exchanger 134. During this process, the CO.sub.2 stream 130 is cooled, and the sorbent material is sufficiently heated up to undergo the desorption phase III. During this process, the temperature of the stream 130 is reduced and any steam that was not condensed in 122 is condensed in this heat exchange process in the tower 108. The mixture 136 consisting of cool CO.sub.2 and any condensed water exit the heat exchanger 134 and may optionally enter a heat exchanger 138 in order to bring the CO.sub.2 stream to ambient temperature. In this heat exchanger 138, the stream 136 is brought in contact with a cold surface, where the source of the low temperature may be ambient air or a stream of water form a nearby water source. This low temperature water may be fresh water or salty ocean or ground water. If any more uncondensed steam has remained in the stream 136, that residual steam is condensed in the heat exchanger 138. After cooling, the stream 140 enters a phase separator 142 (where heat exchanger 138 is absent, stream 136 directly enters the separator 142), where the liquid stream 144 is separated from the vapor stream 146, and the cold water stream 144 then enters a heat exchanger 148 to cool the sorbent material in tower 114 after desorption during phase IV of the process 100. If necessary, cold fresh water 156 may be added to the stream 144 by the means of shut off valve 154. The water exiting the valve 154 may be delivered at the required process pressure. This cold fresh water 156 can be sourced from a local fresh water source, such as a lake or ground water. Using the cold water stream 144 to cool off the sorbent material during phase IV advantageously allows to recover the heat accumulated during the desorption phase III, leading to reduced energy consumption in the exemplary process 100. In the meantime, the still pressurized warm water stream 150 that absorbed the heat from the sorbent material in the heat exchanger 148 is expanded in an expansion device 152 to a pressure ratio that is similar to the pressure ratio across the expansion device 132 and is reverse of the ratio in the compression device 118. In one example, the pressure ratio in 152 is from about 1.01:1 to about 20:1, or from about 1.05:1 to about 2:1, and the temperature of the warm water stream 160 exiting the expansion device 152 is generally lower than the temperature of the water stream 158 exiting the expansion device 132. The mixed amounts of the warm water stream 158 and the warm water stream 160 form a warm water stream 162 that is fed to the cold side of the heat exchanger 122, to form a stream of steam 112 that is fed to the tower 110 in the phase III of the process 100. In this process, the high pressure and high temperature stream 120 heats and evaporates the low pressure and low temperature water stream 162 to form steam 112, while condensing in the heat exchanger 122. In this manner, the water in the process 100 is reused and recycled, with the fresh water 156 being added as needed to compensate any losses. Excess water may also be removed from the system 100, by turning the valve 154 in the opposite direction. In one example, the pressure ratio in the system 100 (the pressure generated by compressor 118 and then released by valves 132 and 152) is set such that the condensing (slightly below boiling) temperature of the pressurized steam 120 is from about 1 K to about 50 K (or from about 1 K to about 5 K) greater than the evaporating (slightly above boiling) temperature of the warm water 162.

(35) The vapor phase 146 exiting the phase separator 142 consists mainly of cold CO.sub.2. This cold CO.sub.2 stream may enter compressor 164 and then exit the system as a compressed CO.sub.2 stream 166. The exit pressure of stream 166 may be from about 1 to about 300 bar. The CO.sub.2 compressor 164 can integrate intercooling stages for increased performance and the heat dissipated in the intercooling stages transferred to pre-heat cold streams in process 100, such as feed water streams 156 or 144. That is, the pure or nearly pure CO.sub.2 can be obtained in the form of a gas, a pressurized liquid, or be expanded to near ambient temperature after compression and cooling and be obtained as a dry ice (maintaining a temperature of about −78° C. at 1 atm.), depending on the utilization and/or sequestration needs. In some embodiments, the CO.sub.2 in stream 166 is about 90 wt. %, about 95 wt. %, or about 99 wt. % pure. The CO.sub.2 may be sequestered or used to prepare a synthesis gas or liquid, or converted to another chemical compound, for example, acetic acid. The CO.sub.2 may be used to grow plants or seaweed, which are subsequently used to prepare a biofuel, such as methanol, ethanol, or butanol, or a mixture thereof.

OTHER EMBODIMENTS

(36) It is to be understood that while the present application has been described in conjunction with the detailed description thereof, the foregoing description is intended to illustrate and not limit the scope of the present application, which is defined by the scope of the appended claims. Other aspects, advantages, and modifications are within the scope of the following claims.