Noble metal catalysts and processes for reforming of methane and other hydrocarbons
Processes for converting methane and/or other hydrocarbons to synthesis gas (i.e., a gaseous mixture comprising H 2 and CO) are disclosed, in which at least a portion of the hydrocarbon(s) is reacted with CO 2 . At least a second portion of the methane may be reacted with H 2 O (steam), thereby improving overall thermodynamics of the process, in terms of reducing endothermicity (ΔH) and the required energy input, compared to “pure” dry reforming in which no H 2 O is present. Catalysts for such processes advantageously possess high activity and thereby can achieve significant levels of methane conversion at temperatures below those used conventionally under comparable conditions. These catalysts also exhibit high sulfur tolerance, in addition to reduced rates of carbon (coke) formation, even in the processing (reforming) of heavier (e.g., naphtha boiling-range or jet fuel boiling-range) hydrocarbons. The robustness of the catalyst translates to high operating stability. A representative catalyst comprises 1 wt-% Pt and 1 wt-% Rh as noble metals, on a cerium oxide support.
1. A CO 2 -steam reforming process comprising contacting a gaseous mixture consisting essentially of one or more hydrocarbons including methane, together with CO 2 and H 2 O as oxidants, with a catalyst to produce a stream of a synthesis gas product having a molar H 2 :CO ratio of at least about 1.5:1,
wherein the catalyst comprises platinum (Pt) in an amount from about 0.3 wt-% to about 3 wt-% on a solid support comprising at least about 80 wt-% of cerium oxide, in combination with one or more other metal oxides, and
wherein, under said reforming conditions, a conversion of the methane is at least about 75% by reaction with CO 2 and H 2 O as the oxidants, and
wherein said molar H 2 :CO ratio and said conversion of methane are maintained for an operating period of at least 500 hours of continuous or discontinuous operation, without undergoing regeneration over said operating period.
2. The process of claim 1 , wherein the catalyst comprises Pt in an amount from about 0.5 wt-% to about 2 wt-%.
3. The process of claim 1 , wherein the molar H 2 :CO ratio, wherein said conversion of methane, which is maintained over said operating period, is at least about 85%.
4. The process of claim 1 , said gaseous mixture consisting essentially of (i) from about 5 mol-% to about 85 mol-% of said one or more hydrocarbons including methane, (ii) from about 8 mol-% to about 90 mol-% of said CO 2 , and (iii) from about 15 mol-% to about 70 mol-% of said H 2 O.
5. The process of claim 1 , wherein a balance of the gaseous mixture includes H 2 S and/or other sulfur-bearing contaminants.
6. The process of claim 1 , wherein said methane is from a renewable source.
7. The process of claim 1 , wherein the contacting is performed by flowing the gaseous mixture through a reactor vessel containing the catalyst, at a weight hourly space velocity (WHSV), based on a weight flow of the gaseous mixture divided by a weight of the catalyst, from about 0.1 hr −1 to about 2.5 hr −1 , to provide the synthesis gas product as an effluent from the reactor vessel.
8. The process of claim 1 , wherein said one or more other metal oxides of the solid support are one or more of aluminum oxide, silicon oxide, titanium oxide, magnesium oxide, and strontium oxide.
9. The process of claim 8 , wherein the one or more other metal oxides is aluminum oxide.
10. The process of claim 1 , wherein the temperature of the catalyst, during said operating period, is not raised by more than 25° C. (45° F.).
11. A CO 2 -steam reforming process comprising contacting a stream of a gaseous mixture comprising one or more hydrocarbons including methane, together with CO 2 and H 2 O as oxidants, with a catalyst to produce a stream of a synthesis gas product, the process further comprising:
determining a molar H 2 :CO ratio of the synthesis gas product and, based on the molar H 2 :CO ratio, adjusting a molar H 2 O:CO 2 ratio of the gaseous mixture toward a target molar H 2 :CO ratio of the synthesis gas product,
wherein the contacting is performed under reforming conditions including a weight hourly space velocity (WHSV), based on a weight flow of the gaseous mixture divided by a weight of the catalyst, from about 0.1 hr −1 to about 2.5 hr −1 ,
wherein the catalyst comprises platinum (Pt) in an amount from about 0.3 wt-% to about 3 wt-% on a solid support comprising at least about 80 wt-% of cerium oxide, in combination with one or more other metal oxides selected from the group consisting of aluminum oxide, silicon oxide, titanium oxide, magnesium oxide, and strontium oxide, and
wherein, under said reforming conditions, a conversion of the methane is at least about 75% by reaction with CO 2 and H 2 O as the oxidants.
12. The process of claim 11 , wherein the reforming conditions include a temperature from about 677° C. (1250° F.) to about 816° C. (1500° F.).
13. The process of claim 11 , wherein said one or more other metal oxides of the solid support is aluminum oxide.
14. The process of claim 11 , wherein the cerium oxide is present in an amount of at least 95% by weight of the solid support.
15. The process of claim 14 , wherein the one or more other metal oxides of the solid support is aluminum oxide.
16. The process of claim 11 , wherein the catalyst comprises Pt in an amount from about 0.5 wt-% to about 2 wt-%.
17. The process of claim 11 , wherein the target molar H 2 :CO ratio of the synthesis gas product is from about 1.5:1 to about 2.3:1.
18. The process of claim 11 , wherein the Pt has a particle size from about 0.3 to about 20 nm.
19. A CO 2 -steam reforming process comprising contacting a gaseous mixture comprising one or more hydrocarbons including methane, together with CO 2 and H 2 O as oxidants, with a catalyst to produce a stream of a synthesis gas product having a molar H 2 :CO ratio of at least about 1.5:1,
wherein the catalyst comprises platinum (Pt) in an amount from about 0.3 wt-% to about 3 wt-% on a solid support comprising at least about 80 wt-% of cerium oxide, in combination with one or more other metal oxides, and
wherein, under said reforming conditions, a conversion of the methane is at least about 75% by reaction with CO 2 and H 2 O as the oxidants,
wherein said molar H 2 :CO ratio and said conversion of methane are maintained for an operating period of at least 500 hours of continuous or discontinuous operation, without undergoing regeneration over said operating period, and
wherein said CO 2 -steam reforming process is endothermic.
20. The process of claim 19 , wherein said one or more other metal oxides of the solid support are one or more of aluminum oxide, silicon oxide, titanium oxide, magnesium oxide, and strontium oxide.
21. The process of claim 20 , wherein the one or more other metal oxides is aluminum oxide.