Materials, methods, and systems for reactive capture and conversion of CO
The present disclosure relates to a composition that includes a first oxide that includes zinc, aluminum, and copper; and a metal that includes least one of an alkali metal and/or an alkaline earth metal, where the composition has a first total uptake capacity of CO 2 of greater than 218 μmol CO 2 /g of composition at a first temperature of about 40° C., a second total uptake capacity of CO 2 of greater than 76 μmol CO 2 /g of composition at a second temperature of about 300° C., and the composition is capable of converting CO 2 to at least one of CO, methane, or methanol, when exposed to H 2 at a third temperature greater than the first temperature.
1 . A composition comprising:
an oxide comprising zinc, aluminum, and copper; and
sodium at a concentration between 5 wt % and 10 wt % present as Na 2 O dispersed on the oxide, wherein:
the composition is capable of reversibly capturing CO 2 .
2 . The composition of claim 1 , wherein the oxide comprises CuO, ZnO, and Al 2 O 3 .
3 . The composition of claim 2 , wherein at least a portion of the oxide is in a crystalline phase.
4 . The composition of claim 1 , wherein the Na 2 O is amorphous.
5 . A method for reducing CO 2 , utilizing a solid composition, the method comprising:
a first contacting of the solid composition with CO 2 at a first temperature and a first pressure, resulting in chemisorption of the CO 2 onto the composition; and
a second contacting of the solid composition with H 2 at a second temperature and a second pressure, resulting in a portion of the chemisorbed CO 2 reacting to form at least one of CO, methane, or methanol, wherein:
the solid composition comprises:
an oxide comprising zinc, aluminum, and copper; and
sodium at a concentration between 5 wt % and 10 wt % present as Na 2 O dispersed on the oxide;
the first temperature is between 0° C. and 450° C.,
the first pressure is between 0.8 bar and 30 bar (absolute),
the second temperature is between 50° C. and 450° C., and
the second pressure is between 0.8 bar and 30 bar (absolute).
6 . The composition of claim 1 , further comprising:
a first total uptake capacity of CO 2 of greater than 218 μmol CO 2 /g of composition at a first temperature of about 40° C., and
a second total uptake capacity of CO 2 of greater than 76 μmol CO 2 /g of composition at a second temperature of about 300° C., wherein:
the composition is capable of converting CO 2 to at least one of CO, methane, or methanol, when exposed to H 2 at a third temperature greater than the first temperature.
7 . The composition of claim 6 , wherein the first total uptake capacity is between 218 μmol CO 2 /g of composition and 300 μmol CO 2 /g of composition.
8 . The composition of claim 6 , wherein the second total uptake capacity is between 76 μmol CO 2 /g of composition and 250 μmol CO 2 /g of composition.
9 . The method of claim 5 , wherein the solid composition is positioned within at least one packed bed reactor.
10 . The method of claim 9 , wherein the first contacting is completed by providing the CO 2 in a continuous flow to the packed bed reactor.
11 . The method of claim 9 , wherein the CO 2 is provided to the packed bed reactor in a gas stream at a molar concentration between 0.2 mol % and 100 mol % CO 2 .
12 . The method of claim 9 , wherein the second contacting is completed by providing the H 2 in a continuous flow to the packed bed reactor.
13 . The method of claim 9 , wherein the H 2 and chemisorbed CO 2 are provided at a molar ratio of H 2 :CO 2 between 1:1 and 10:1.
14 . The method of claim 9 , further comprising:
a separating, wherein:
during the second contacting, a first stream comprising H 2 , CO 2 , and methanol and at least one of CO or methane exit the packed bed reactor,
the first stream is directed to the separating, which separates the first stream into a second stream comprising methanol and a third stream comprising H 2 and CO 2 , and
at least one of CO or methane, and the third stream is recycled to the second contacting.
15 . The method of claim 9 , further comprising:
a reacting; and
a separating, wherein:
during the second contacting, a first stream comprising H 2 and CO 2 , and at least one of CO or methane exit the packed bed reactor,
the first stream is directed to the reacting resulting in at least a portion of the H 2 and CO 2 , and at least one of the CO or methane reacting to form a second stream comprising methanol,
the second stream is directed to the separating, which separates the second stream into a third stream comprising methanol and a fourth stream comprising H 2 and CO 2 , and at least one of CO or methane, and the fourth stream is recycled to the second contacting.