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Disclosed is a process for converting synthesis gas to liquid hydrocarbon mixtures useful in the production of fuels and petrochemicals. The synthesis gas is contacted with at least two layers of synthesis gas conversion catalyst wherein each synthesis gas conversion catalyst layer is followed by a

Disclosed is a process for converting synthesis gas to liquid hydrocarbon mixtures useful in the production of fuels and petrochemicals. The synthesis gas is contacted with at least two layers of synthesis gas conversion catalyst wherein each synthesis gas conversion catalyst layer is followed by a layer of hydrocracking catalyst and hydroisomerization catalyst or separate layers of hydrocracking and hydroisomerization catalysts. The process can occur within a single reactor, at an essentially common reactor temperature and an essentially common reactor pressure. The process provides a high yield of naphtha range liquid hydrocarbons and a low yield of wax.

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1. A process for converting synthesis gas to a hydrocarbon mixture comprising contacting a feed comprising a mixture of carbon monoxide and hydrogen with at least two layers of synthesis gas conversion catalyst particles including a metal component, and at least two layers containing hydrocracking c

1. A process for converting synthesis gas to a hydrocarbon mixture comprising contacting a feed comprising a mixture of carbon monoxide and hydrogen with at least two layers of synthesis gas conversion catalyst particles including a metal component, and at least two layers containing hydrocracking catalyst particles including an acidic component and hydroisomerization catalyst particles, in an alternating arrangement within a single reactor tube, such that the feed contacts at least a first synthesis gas conversion catalyst layer, a first hydrocracking and hydroisomerization catalyst layer, a second synthesis gas conversion catalyst layer and a second hydrocracking and hydroisomerization catalyst layer sequentially, thereby resulting in a hydrocarbon mixture which at ambient conditions contains: 0-20 weight % CH4;0-20 weight % C2-C4;greater than 70% C5+; and40-80 weight % C5-C12. 2. The process of claim 1 wherein the process occurs at an essentially common reactor temperature and an essentially common reactor pressure. 3. The process of claim 1 wherein the hydrocarbon mixture further contains 0-5 weight % C21+ normal paraffins. 4. The process of claim 1 wherein each of the synthesis gas conversion catalyst particles and the hydrocracking catalyst particles have an average particle diameter, respectively, and each synthesis gas conversion catalyst layer has a thickness at least two times the average particle diameter of the synthesis gas conversion catalyst particles, and each hydrocracking and hydroisomerization catalyst layer has a thickness at least two times the average particle diameter of the hydrocracking and hydroisomerization catalyst particles. 5. The process of claim 4 wherein the particle diameter of each of the synthesis gas conversion catalyst particles and the hydrocracking catalyst particles is between about 1 mm and about 5 mm. 6. The process of claim 1 wherein the weight ratio of the acidic component of the hydrocracking catalyst and the isomerization component of the hydroisomerization catalyst to the metal component of the synthesis gas conversion catalyst is between 2:1 and 100:1. 7. The process of claim 1 wherein the synthesis gas conversion catalyst comprises cobalt on a solid oxide support. 8. The process of claim 1 wherein the synthesis gas conversion catalyst comprises ruthenium on a solid oxide support. 9. The process of claim 7 or 8 wherein the solid oxide support is selected from the group consisting of alumina, silica, titania, magnesia, zirconia, chromia, thoria, boria and mixtures thereof. 10. The process of claim 1 wherein the synthesis gas conversion catalyst further comprises an acidic component. 11. The process of claim 10 wherein the weight ratio of the acidic component of the hydrocracking catalyst to the metal component of the synthesis gas conversion catalyst is between 0.1:1 and 100:1. 12. The process of claim 1 wherein the hydrocracking catalyst is selected from the group consisting of amorphous silica-alumina, tungstated zirconia, zeolitic crystalline medium pore molecular sieves, non-zeolitic crystalline medium pore molecular sieves, zeolitic crystalline large and extra large pore molecular sieves, non-zeolitic crystalline large and extra large pore molecular sieves, mesoporous molecular sieves and zeolite analogs. 13. The process of claim 1 wherein the reactor temperature is between about 160° C. and about 300° C. 14. The process of claim 1 wherein the synthesis gas conversion catalyst further comprises a promoter selected from the group consisting of Mn, Pr, Rh, Pt, Pd, Cu, Ag, Au, Zn, Cd, Re, Ni, K, Cr, Zr, and Ce. 15. The process of claim 1 wherein the synthesis gas conversion catalyst further comprises a promoter selected from the group consisting of magnesium oxides, lanthanum oxides, manganese oxides, zirconium oxides and titanium oxides. 16. The process of claim 1 wherein the reactor pressure is between about 3 atmospheres and about 35 atmospheres. 17. The process of claim 1 wherein the hydrocarbon mixture is substantially free of solid wax at ambient conditions. 18. The process of claim 1 wherein the hydrocarbon mixture has a cloud point no greater than 15° C. 19. A process for converting synthesis gas to a hydrocarbon mixture comprising contacting a feed comprising a mixture of carbon monoxide and hydrogen with at least two layers of synthesis gas conversion catalyst particles including a metal component, at least two layers of hydrocracking catalyst particles including an acidic component, and at least two layers of hydroisomerization catalyst particles, in an alternating layer arrangement within a single reactor tube, such that the feed contacts a first synthesis gas conversion catalyst layer, a first hydrocracking catalyst layer, a first hydroisomerization catalyst layer, a second synthesis gas conversion catalyst layer, sequentially, followed by a second hydrocracking catalyst layer and a second hydroisomerization catalyst layer, in any order, thereby resulting in a hydrocarbon mixture which at ambient conditions contains: 0-20 weight % CH4;0-20 weight % C2-C4;greater than 70% C5+; and40-80 weight % C5-C12. 20. A process for converting synthesis gas to a hydrocarbon mixture comprising contacting a feed comprising a mixture of carbon monoxide and hydrogen with at least two layers of synthesis gas conversion catalyst particles including a metal component, at least two layers of hydrocracking catalyst particles including an acidic component, and at least two layers of hydroisomerization catalyst particles, in an alternating layer arrangement within a single reactor tube, such that the feed contacts a first synthesis gas conversion catalyst layer, a first hydroisomerization catalyst layer, a first hydrocracking catalyst layer, a second synthesis gas conversion catalyst layer, sequentially, followed by a second hydrocracking catalyst layer and a second hydroisomerization catalyst layer, in any order, thereby resulting in a hydrocarbon mixture which at ambient conditions contains: 0-20 weight % CH4;0-20 weight % C2-C4;greater than 70% C5+; and40-80 weight % C5-C12.