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The present invention provides methods, reactor systems, and catalysts for increasing the yield of aromatic hydrocarbons produced while converting alkanols to hydrocarbons. The invention includes methods of using catalysts to increase the yield of benzene, toluene, and mixed xylenes in the hydrocarb

The present invention provides methods, reactor systems, and catalysts for increasing the yield of aromatic hydrocarbons produced while converting alkanols to hydrocarbons. The invention includes methods of using catalysts to increase the yield of benzene, toluene, and mixed xylenes in the hydrocarbon product.

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1. A method of converting alkanols to aromatic hydrocarbons comprising: partially dehydrogenating a C1-C6 alkanol feedstock in the presence of a dehydrogenation catalyst at an effective dehydrogenation temperature and dehydrogenation pressure to produce hydrogen and a mixture of oxygenate components

1. A method of converting alkanols to aromatic hydrocarbons comprising: partially dehydrogenating a C1-C6 alkanol feedstock in the presence of a dehydrogenation catalyst at an effective dehydrogenation temperature and dehydrogenation pressure to produce hydrogen and a mixture of oxygenate components comprising (a) unreacted C1-C6 alkanol and (b) a carboxylic acid, an aldehyde, an ester or any combination thereof; wherein at least a portion of the oxygenate components in the mixture have a hydrogen to carbon effective ratio of less than 1.6 and wherein the extent of partial dehydrogenation results in the mixture of oxygenate components having a total hydrogen to carbon effective ratio of between 1.0 and 1.5; andexposing the mixture of oxygenate components to a zeolite oxygenate conversion catalyst at an oxygenate conversion temperature and an oxygenate conversion pressure to produce aromatic hydrocarbons. 2. The method of claim 1 wherein the mixture of oxygenate components has a total hydrogen to carbon effective ratio of between 1.2 and 1.5. 3. The method of claim 1 wherein greater than 40% of carbon in the alkanol feedstock is contained within the aromatic hydrocarbons. 4. The method of claim 1 wherein greater than 45% of carbon in the alkanol feedstock is contained within the aromatic hydrocarbons. 5. The method of claim 1 wherein a portion of the alkanol feedstock is less than about 100 years old as calculated from the carbon 14 concentration of the alkanol feedstock. 6. The method of claim 1 wherein the alkanol feedstock comprises a primary alcohol. 7. The method of claim 6 wherein the alkanol feedstock comprises ethanol. 8. The method of claim 1 wherein the alkanol comprises n-butanol. 9. The method of claim 1 wherein the dehydrogenation catalyst comprises a metal selected from the group consisting of Cu, Ru, Ag, CuCr, CuZn, Co, Raney copper, copper-zinc-aluminate, alloys thereof, and combinations thereof. 10. The method of claim 1 wherein the dehydrogenation catalyst further comprises a support. 11. The method of claim 10 wherein the support comprises a material selected from the group consisting of alumina, silica, silica-alumina, titania, carbon, zirconia, zinc aluminate, and mixtures thereof. 12. The method of claim 10 wherein the dehydrogenation catalyst comprises Cu on a silica support. 13. The method of claim 1 wherein the dehydrogenation temperature is between about 80° C. and 500° C. 14. The method of claim 1 wherein the dehydrogenation pressure ranges from below atmospheric pressure to about 1000 psig. 15. The method of claim 1 wherein the zeolite oxygenate conversion catalyst is ZSM-5. 16. The method of claim 1 wherein the zeolite oxygenate conversion catalysts is modified by a material selected from the group consisting of phosphorous, gallium, zinc, nickel, tungsten, and mixtures thereof. 17. The method of claim 1 wherein the zeolite oxygenate conversion catalyst contains a binder selected from the group consisting of alumina, silica, silica-alumina, titania, zirconia, aluminum phosphate, and mixtures thereof. 18. The method of claim 1 wherein the oxygenate conversion temperature is between about 250° C. and 550° C. 19. The method of claim 1 wherein the oxygenate conversion pressure ranges from less than atmospheric pressure to about 1000 psig. 20. The method of claim 1 wherein the dehydrogenation catalyst and the oxygenate conversion catalyst are combined in a multi-functional dehydrogenation/oxygenate conversion catalyst. 21. A method of converting ethanol to aromatic hydrocarbons comprising: partially dehydrogenating an ethanol feedstock in the presences of a dehydrogenation catalyst at an effective dehydrogenation temperature and dehydrogenation pressure to produce a mixture of oxygenate components comprising ethanol, acetaldehyde, acetic acid, and ethyl acetate, wherein the extent of partial dehydrogenation results in the mixture of oxygenate components having a total hydrogen to carbon effective ratio of between 1.0 and 1.5;exposing the mixture of oxygenate components to a zeolite oxygenate conversion catalyst at an oxygenate conversion temperature and an oxygenate conversion pressure to produce aromatic hydrocarbons. 22. A method of converting alkanols to aromatic hydrocarbons comprising: partially dehydrogenating a C1-C6 alkanol feedstock in the presence of a dehydrogenation catalyst at an effective dehydrogenation temperature and dehydrogenation pressure to produce hydrogen and a mixture of oxygenate components comprising (a) unreacted C1-C6 alkanol and (b) a carboxylic acid, an aldehyde, an ester, or any combination thereof; wherein at least a portion of the oxygenate components in the mixture have a hydrogen to carbon effective ratio of less than 1.6 and wherein the extent of partial dehydrogenation results in the mixture of oxygenate components having a total hydrogen to carbon effective ratio of between 1.0 and 1.5;separating the mixture of oxygenate components into a first oxygenate stream having a total hydrogen to carbon effective ratio of between 1.0 and 1.5 and a second oxygenate stream;exposing the first oxygenate stream to an a zeolite conversion catalyst at an oxygenate conversion temperature and an oxygenate conversion pressure to produce aromatic hydrocarbons; andexposing the second oxygenate stream to the dehydrogenation catalyst at an effective dehydrogenation temperature and dehydrogenation pressure to produce hydrogen and an additional mixture of oxygenate components.