Autothermal reactor and method for production of synthesis gas
An autothermal reactor and method for producing synthesis gas in which a heated oxygen containing stream is expanded into a mixing chamber to entrain a hydrocarbon containing stream to form a reactant stream without reaction of the oxygen and hydrocarbon contents of the streams. The reactant stream is reacted in a series of sequential catalytic reaction zones to react the hydrocarbon and oxygen contained in the reactant stream to form the synthesis gas. The sequential catalytic reaction zones are configured such that an initial partial oxidation reaction occurs that is followed by endothermic reforming reactions having ever decreasing temperatures. The sequential catalytic reaction zones in which the endothermic reforming reactions occur contain a precious metal catalyst supported on ceramic supports that have successively greater surface areas to compensate for the temperature decrease while remaining stable and without a transform in state.
1. An autothermal reactor for producing synthesis gas comprising:
a primary mixing chamber having an orifice to expand a heated oxygen containing stream into said mixing chamber and an inlet located adjacent to said orifice and oriented to introduce a hydrocarbon containing stream into the mixing chamber tangentially to said heated oxygen containing stream such that said hydrocarbon containing stream is entrained in said heated oxygen containing stream to mix oxygen in said heated oxygen containing stream with hydrocarbons contained in said hydrocarbon containing stream at a sufficiently rapid rate so as not to react the oxygen and the hydrocarbons, thereby to produce a reactant stream made up of an unreacted mixture of the heated oxygen containing stream and the hydrocarbon containing stream;
an initial partial oxidation reaction zone having a supported partial oxidation catalyst on a monolithic support, said initial partial oxidation reaction zone in communication with said mixing chamber and followed by at least two endothermic reforming reaction zones heated by an exothermic reaction of said partial oxidation reaction zone to react the oxygen and the hydrocarbons of said reactant stream and thereby to form said synthesis gas;
a secondary mixing chamber situated between said partial oxidation reaction zone and said at least two endothermic reforming zones, said secondary mixing chamber having a secondary inlet to receive a recycle stream containing synthesis gas components obtained by separation of hydrogen and carbon monoxide from said synthesis gas; and
the at least two endothermic reforming reaction zones formed of beds of pellets containing a precious metal catalyst supported on supports formed of different materials that provide a greater surface area for a successive of the at least two endothermic reforming reaction zones than an initial of the at least two endothermic reforming reaction zones directly following the partial oxidation reaction zone, the initial and the successive of the at least two endothermic reforming reaction zones configured to operate at ever decreasing operational temperatures such that a material making up a support of the successive of the at least two endothermic reforming reaction zones remains stable.
2. The reactor of claim 1 , wherein:
said mixing chamber is defined by an inner surface outwardly diverging from said orifice to form a frustum of a cone; and
said surface outwardly diverging from said orifice at an angle calculated to inhibit re-circulation within said mixing chamber.
3. The reactor of claim 1 , further comprising a ceramic heat shield of honeycomb configuration located between the partial oxidation reaction zone and the mixing chamber to inhibit heat transfer from the partial oxidation reaction zone to the mixing chamber.
4. The reactor of claim 1 , wherein said monolith is of honeycomb configuration and said pellets of the initial of the at least two endothermic reforming reaction zones is formed by alpha-alumina and the successive of the at least two endothermic reforming reaction zones is formed by gamma-alumina, respectively.
5. The reactor of claim 1 , wherein said mixing chamber, said partial oxidation reaction zone and said at least two endothermic reforming zones are in an inline relationship.
6. The reactor of claim 1 , wherein the initial of said endothermic reforming reaction zones has a surface area from between about 0.1 and about 10 m 2 /gm and the successive of the at least two endothermic reforming zones has surface areas from between about 5 and about 300 m 2 /gm.
7. The reactor of claim 1 , wherein said precious metal catalyst is Pt, Rh, Ru, Pd, or Ni.
8. The reactor of claim 1 , wherein the monolithic support is formed from a ceramic doped with a partial oxidation catalyst.