Reactor, CO
A reactor and process for production of hydrogen gas from a carbon-containing fuel in a reaction that generates carbon dioxide is described. The carbon-containing fuel can be, for example, carbon monoxide, alcohols, oxygenates bio-oil, oil and hydrocarbons. In preferred embodiments, the reactor includes a monolithic structure form with an array of parallel flow channels. Methods of using the reactor are also described. In the reactor apparatus of the present invention, the catalytic reaction for hydrogen formation is conducted in conjunction with a carbonation reaction that removes carbon dioxide that is produced by the reactor. The carbonation reaction involves reaction of the carbon dioxide produced from the hydrogen formation reaction with metal oxide-based sorbents. The reactor apparatus can be periodically regenerated by regeneration of the sorbent. A carbon dioxide sorbent system comprising a solid sorbent and a eutectic, mixed alkali metal molten phase is also described.
1. A reactor for producing hydrogen, comprising:
a plurality of reaction channels comprising a steam reforming catalyst or water gas shift catalyst, each reaction channel comprising one or more channel walls;
wherein at least one reaction channel wall is porous to carbon dioxide;
at least one sorbent chamber adjacent the reaction channel, separated from the reaction channel by one or more channel walls and comprising a CO2 sorbent; and
wherein the reaction channel comprising the steam reforming catalyst has an average diameter of between 0.1 mm and 10 mm,
wherein the reactor channels each have an inlet and an outlet, and
wherein the sorbent chamber(s) have no ports or closed ports configured such that gaseous flow into and out of a sorbent chamber is only through the porous reaction channel wall(s).
2. The reactor of claim 1 wherein the reactor comprises at least 10 parallel reaction channels.
3. The reactor of claim 1 wherein the catalyst is a steam reforming catalyst and wherein the steam reforming catalyst is a wall coating and wherein an open bulk flow path is present in reaction channel.
4. The reactor of claim 3 wherein the steam reforming catalyst comprises Ni, Cu, Mg, Ce, and Al.
5. The reactor of claim 1 wherein the reactor comprises a honeycomb monolith.
6. The reactor of claim 5 comprising a plurality of parallel reaction channels alternating with plurality of parallel sorbent chambers; preferably at least 10 parallel reaction channels alternating with at least 10 parallel sorbent chambers.
7. The reactor of claim 1 wherein sorbent fills a cross-section of the sorbent chamber.
8. The reactor of claim 1 wherein the reactor comprises a honeycomb monolith; and wherein the monolith comprises: a macro- and meso-porous material; a metal oxide; titania, alumina, silica; or a dense material such as metal with apertures for gas flow.
9. The reactor of claim 1 wherein the sorbent surrounds at least one reaction channel.
10. The reactor of claim 1 wherein a single sorbent chamber surrounds the plurality of reaction channels.
11. The reactor of claim 1 wherein the porous channel wall has a volume average pore size that in the range of about 1 nm to 100 μm.
12. A method of steam reforming, comprising passing hydrocarbon and steam into the reactor of claim 1 .
13. A method of converting hydrocarbons to H2, comprising
passing a carbon fuel and water into the reactor of claim 1 ;
wherein the water is in the form of steam or wherein the water is converted to steam within the reactor;
wherein the reaction channel is at a temperature of at least 350 °C.;
wherein the steam and carbon fuel react in the reaction channel at a temperature of at least 350 °C. to produce at least H 2 and CO 2 ;
wherein at least a portion of the CO 2 flows into the sorbent chamber where it is sorbed by the CO 2 sorbent; and
regenerating the CO 2 sorbent.
14. The method of claim 13 wherein the carbon fuel is a hydrocarbon and wherein the reactor comprises a steam reforming catalyst.
15. The method of claim 14 wherein the reforming and sorption are performed at a temperature less than or equal to about 700° C., in some embodiments less than or equal to about 550° C. in a time of less than about 10 minutes.
16. The method of claim 14 wherein the reforming and sorption are performed iteratively in a plurality of cycles with a delay between any subsequent cycle of less than or equal to about 10 minutes.
17. The method of claim 14 wherein the hydrocarbon feedstock is a bio-oil.