초록

A method for the thermo-neutral reforming of liquid hydrocarbon fuels which employs a Ni—Ce2O—Pt—Rh catalyst having dual functionalities to achieve both combustion and steam reforming.

대표청구항 ▼

We claim: 1. A single stage thermo-neutral reforming process for the production of a hydrogen-rich synthesis gas from liquid hydrocarbon fuels, which comprises: a) providing a mixture of a liquid hydrocarbon fuel, air and steam to an interior zone of a reactor, said interior zone including a cataly

We claim: 1. A single stage thermo-neutral reforming process for the production of a hydrogen-rich synthesis gas from liquid hydrocarbon fuels, which comprises: a) providing a mixture of a liquid hydrocarbon fuel, air and steam to an interior zone of a reactor, said interior zone including a catalyst bed consisting of a Ni—Ce2O3—Pt−Rh combined combustion and steam and/or CO2 reforming catalyst; b) pre-heating the mixture at a temperature of about 380° C. to about 450° C. to form a vapor; and, c) bringing the heated vaporized mixture into contact with the catalyst bed at a gas hour space velocity of about 25,000 h−1 or greater causing an exothermic combustion reaction raising the reaction temperature to about 800° C. to about 900° C. and also causing an endothermic steam reforming reaction for a period of time sufficient to reform the liquid fuel to yield a hydrogen-rich synthesis gas. 2. The process of claim 1, wherein the liquid hydrocarbon fuel is a petroleum-based fuel. 3. The process of claim 2, wherein the petroleum-based liquid is selected from the group consisting of iso-octane, light naphtha, heavy-naphtha, kerosene and diesel. 4. The process of claim 1, wherein the gas hour space velocity is between about 25,000 and about 40,000 h−1. 5. The process of claim 1, wherein the pre-heating temperature is from about 410° C. to about 420° C. 6. The process of claim 1, wherein the heat generated from the exothermic combustion reaction is neutralized and compensated by the endothermic reaction on the same catalyst bed. 7. The process of claim 1, wherein the reaction is carried out without the need of an external heat supply. 8. The process of claim 1, wherein coke formation is avoided. 9. The process of claim 3, wherein over 96.5% of iso-octane and light naphtha feedstocks are converted into syngas (H2ZCOZCO2ZCl—I4). 10. The process of claim 3, wherein over 99% of heavy naphtha feedstock is converted into syngas (H2ZCOZCO2ZCH4). 11. The process of claim 1, wherein the syngas produced from the process can be further purified to produce highly pure hydrogen. 12. The process of claim 1, wherein the hydrogen rich syngas is used as a feed for on-board reformers in vehicles incorporating a high temperature or low temperature fuel cell. 13. The process of claim 1, wherein the hydrogen-rich syngas is used as a feed for hydrogen enrichment in internal combustion engines. 14. The process of claim 1, wherein the hydrogen-rich syngas is employed in stationary applications. 15. The process of claim 1, wherein the sulfur content of the liquid hydrocarbons fuel is 200 ppm or less.