초록

The instant invention relates to a process to produce high octane, low sulfur naphtha products through the removal of basic nitrogen-containing compounds with subsequent skeletal isomerization of feed olefins and hydrotreating.

대표청구항 ▼

The invention claimed is: 1. A process for producing low sulfur naphtha products comprising: a) contacting a naphtha boiling range feedstream containing organically bound sulfur, nitrogen-containing compounds, and olefins in a first reaction zone operated under conditions effective to remove at lea

The invention claimed is: 1. A process for producing low sulfur naphtha products comprising: a) contacting a naphtha boiling range feedstream containing organically bound sulfur, nitrogen-containing compounds, and olefins in a first reaction zone operated under conditions effective to remove at least a portion of said nitrogen-containing compounds with an acidic material to produce a first reaction zone effluent having a reduced amount of nitrogen-containing compounds; b) contacting at least a portion of said first reaction zone effluent in a second reaction zone operated under effective hydroisomerization conditions and in the presence of hydrogen-containing treat gas with a second catalyst comprising ZSM-48 having an alpha value in the range of about 1 to about 100 to produce a second reaction zone effluent; and c) hydrotreating at least a portion of the second reaction zone effluent of step b) above in a third reaction zone operated at effective hydrotreating conditions and in the presence of hydrogen-containing treat gas and a third catalyst selected from hydrotreating catalysts comprising about 0.1 to 27 wt. % of a Group VIII metal oxide, about 1 to 45 wt. % of a Group VI metal oxide, and having a median pore diameter of about 60 Å to about 200 Å to produce a desulfurized product. 2. The process of claim 1 wherein said first reaction zone comprises one or more reactors or reaction zones. 3. The process according to claim 2 wherein said second and third reaction zones comprise one or more catalyst beds selected from the group consisting of fluidized beds, ebullating beds, slurry beds, fixed beds, and moving beds wherein each of said one or more catalyst beds contains a catalyst suitable for the reaction zone in which the catalyst bed is located. 4. The process of according to claim 1 wherein said desulfurized product contains less than 100 wppm sulfur. 5. The process according to claim 3 wherein said second and third reaction zones are located in the same reaction vessel. 6. The process according to claim 5 wherein said second and third reaction zones comprise one or more fixed catalyst beds. 7. The process according to claim 2 wherein said process further comprises interstage cooling between said first, second, and third reaction zones, or between catalyst beds in said first, second, and third reaction zones. 8. The process according to claim 2 wherein said acidic material is selected from Amberlyst, alumina, sulfuric acid, spent sulfuric acid obtained from an alkylation unit, and any other acidic material known to be effective at removing nitrogen compounds from a hydrocarbon stream. 9. The process according to claim 1 wherein said third catalyst is a hydrotreating catalyst comprising about 4 to about 12% of a Group VIII metal oxide and about 10 to about 40 wt. % of a Group VI metal oxide. 10. The process according to claim 1 wherein said third catalyst is a hydrotreating catalyst comprising about 1 to 25 wt. % MoO3, about 0.1 to 6 wt. % CoO wherein said CoO and MoO3 are present in an atomic ratio of about 0.1 to about 1.0 Co/Mo, and said catalyst has a median pore diameter of about 75 Å to about 175 Å, wherein said third catalyst has a MoO3 surface concentration of about 0.5횞10-4 to about 3횞10-4 g/m2 g and an average particle size diameter of less than 2.0 mm. 11. The process according to claim 10 wherein said effective hydroisomerization conditions are selected to cause skeletal isomerization of the olefins present in said naphtha boiling range feedstream. 12. The process according to claim 11 wherein said second reaction zone effluent has a higher ratio of iso-olefins to n-olefins than the naphtha boiling range feedstream. 13. The process according to claim 10 wherein said third catalyst further comprises a suitable binder or matrix material selected from zeolites, alumina, silica, titania, calcium oxide, strontium oxide, barium oxide, carbons, zirconia, diatomaceous earth, lanthanide oxides including cerium oxide, lanthanum oxide, neodymium oxide, yttrium oxide, and praseodymium oxide; chromia, thorium oxide, urania, niobia, tantala, tin oxide, zinc oxide, and aluminum phosphate. 14. The process according to claim 13 wherein said suitable binder or matrix support of said second catalyst also contains less than about 1 wt. % of contaminants, such as Fc, sulfates, silica, and various metal oxides that can be introduced during the preparation of the support. 15. The process according to claim 13 wherein said suitable binder or matrix support of said third catalyst also contains about 0 to 5 wt. % of an additive selected from the group consisting of phosphorus and metals or metal oxides from Group IA (alkali metals) of the Periodic Table of the Elements. 16. The process according to claim 13 wherein said suitable binder or matrix material is selected from alumina, silica, and silica-alumina. 17. The process according to claim 16 wherein said suitable binder or matrix material is alumina. 18. The process according to claim 10 wherein said second catalyst further comprises a suitable porous binder or matrix material selected from clays, silica, and/or metal oxides such as alumina. 19. The process according to claim 18 wherein said suitable porous binder or matrix material is selected from silica, alumina, or a kaolin clay. 20. The process according to claim 19 wherein said suitable porous binder or matrix material is alumina present in a ratio of less than about 15 parts zeolite to one part binder. 21. The process according to claim 20 wherein said effective hydrotreating conditions are selected in such a manner that said desulfurized naphtha product has a sulfur level less than 50 wppm sulfur. 22. The process according to claim 21 wherein said effective hydrotreating conditions are selective hydrotreating conditions. 23. The process according to claim 21 wherein said desulfurized naphtha product has a higher concentration of iso-paraffins than n-paraffins. 24. A process for producing low sulfur naphtha products comprising; a) contacting a naphtha boiling range feedstream containing organically bound sulfur, nitrogen-containing compounds, and olefins in a first reaction zone operated under conditions effective to remove at least a portion of said nitrogen-containing compounds with an acidic material selected from amberlyst and alumina to produce a first reaction zone effluent having less than 50 wppm total nitrogen; b) contacting at least a portion of said first reaction zone effluent in a second reaction zone operated under effective hydroisomerization conditions and in the presence of hydrogen-containing treat gas with a second catalyst comprising at least one zeolite selected from ZSM-23 and ZSM-48 and having an alpha value in the range of about 2 to about 80 to produce a second reaction zone effluent; and c) hydrotreating at least a portion of the second reaction zone effluent of step b) above in a third reaction zone operated under effective hydrotreating conditions and in the presence of hydrogen-containing treat gas and a third catalyst selected from hydrotreating catalysts comprising about 1 to 25 wt. % MoO3, about 0.1 to 6 wt. % CoO wherein said CoO and MoO3 are present in an atomic ratio of about 0.1 to about 1.0 Co/Mo, and said third catalyst has a median pore diameter of about 75 Å to about 175 Å, wherein said third catalyst has a MoO3 surface concentration of about 0.75횞10-4 to about 2.5횞10-4 g/m2 and an average particle size diameter of less than 2.0 mm to produce a desulfurized product having a sulfur level less than 100 wppm sulfur. 25. The process according to claim 24 wherein said first reaction zone effluent contains less than 25 wppm total nitrogen. 26. The process according to claim 25 wherein said second catalyst is ZSM-48. 27. The process according to claim 26 wherein said third catalyst is a hydrotreating catalyst comprising about 2 to 10 wt. % MoO3, about 0.5 to 5.0 wt. % CoO wherein said CoO and MoO3 are present in an atomic ratio of about 0.20 to about 0.80 Co/Mo, and said catalyst has a median pore diameter of about 75 Å to about 175 Å, wherein said second catalyst has a MoO3 surface concentration of about 0.5횞10-4 to about 3횞10-4 g/m2 and an average particle size diameter of less than 1.6 mm. 28. The process according to claim 27 wherein said effective hydroisomerization conditions are selected to cause skeletal isomerization of the olefins present in said naphtha boiling range feedstream. 29. The process according to claim 27 wherein said third catalyst further comprises a suitable binder or matrix material selected from alumina, silica, and silica-alumina. 30. The process according to claim 29 wherein said second catalyst further comprises a suitable porous binder or matrix material selected from clays, silica, and/or metal oxides such as alumina. 31. The process according to claim 30 wherein said second catalyst further comprises alumina present in a ratio of less than about 15 parts zeolite to one part binder. 32. The process according to claim 30 wherein said effective hydrotreating conditions are selected in such a manner that said desulfurized naphtha product has a sulfur level less than 50 wppm sulfur. 33. The process according to claim 32 wherein said effective hydrotreating conditions are selective hydrotreating conditions. 34. The process according to claim 31 wherein said desulfurized naphtha product has a higher concentration of iso-paraffins than n-paraffins. 35. A process for producing low sulfur naphtha products from an olefin and sulfur containing naphtha boiling range feedstream comprising: a) contacting a naphtha boiling range feedstream containing organically bound sulfur, nitrogen-containing compounds, and olefins in a first reaction zone operated under conditions effective to remove at least a portion of said nitrogen-containing compounds with a first catalyst selected from Amberlyst and alumina to produce a first reaction zone effluent having less than 10 wppm total nitrogen; b) contacting said first reaction zone effluent in a second reaction zone operated under effective hydroisomerization conditions selected to cause skeletal isomerization of said olefins contained in said feedstream and in the presence of hydrogen-containing treat gas with a second catalyst comprising ZSM-48 and an alumina binder, wherein said binder and ZSM-48 are present in a ratio of less than about 15 parts zeolite to one part binder, to produce a second reaction zone effluent having a higher ratio of iso-olefins to n-olefins than the naphtha boiling range feedstream; and c) hydrotreating the second reaction zone effluent of step b) above in a third reaction zone operated under selective hydrotreating conditions and in the presence of hydrogen-containing treat gas and a third catalyst selected from supported hydrotreating catalysts comprising about 3 to 6 wt. % MoO3, about 1 to 3 wt. % CoO wherein said CoO and MoO3 are present in an atomic ratio of about 0.25 to about 0.72 Co/Mo, and said third catalyst has a median pore diameter of about 80 Å to about 150 Å, wherein said second catalyst has a MoO3 surface concentration of about 1횞10-4 to 2횞10-4 g/m2 and an average particle size diameter of less than 1.4 mm to produce a desulfurized product having a sulfur level less than 50 wppm sulfur and a higher concentration of iso-paraffins than n-paraffins.