Catalytic pre-reforming process to convert paraffinic hydrocarbons

1. An integrated process for catalytic reforming of hydrotreated naphtha having less than 0.5 ppmw sulfur and nitrogen, the process comprising:

separating a hydrotreated naphtha feedstream into a light naphtha stream and a heavy naphtha stream, wherein the light naphtha stream consists of at least 90 weight % C5-C6 hydrocarbons and is characterized by a first N+2A value where N+2A is a sum of naphthenic compound compositional content and two times aromatic compositional content, and wherein the heavy naphtha stream consists of at least 90 weight % C7-C11 or C7-C12 hydrocarbons;

pre-reforming all or a portion of the light naphtha stream in the presence of hydrogen and an effective pre-reforming dehydrocyclization catalyst to produce a pre-reformed stream having decreased paraffinic content, and an increased naphthenic content and/or aromatic content, relative to the light naphtha stream, and wherein the pre-reformed stream has a second N+2A value that is greater than the first N+2A value;

catalytically reforming the heavy naphtha stream and the pre-reformed stream to produce a reformate stream.

2. The process as in claim 1 , wherein pre-reforming occurs in a unit that is separate from a unit in which catalytic reforming occurs.

3. The process as in claim 1 , wherein pre-reforming and catalytic reforming occur in a common catalytic reforming zone including a pre-reforming reactor in which pre-reforming occurs that us upstream of a catalytic reforming reactor in which catalytic reforming occurs.

4. The process as in claim 1 , further comprising recovering at least a portion of the reformate stream as gasoline blending components, and/or passing at least a portion of the reformate stream to an aromatic complex for recovery of aromatic products.

5. The process as in claim 1 , wherein a temperature cut point between the light naphtha stream and the heavy naphtha stream is about 80-88° C.

6. The process as in claim 1 , wherein a temperature cut point between the light naphtha stream and the heavy naphtha stream is about 80° C.

7. An integrated process for catalytic reforming of hydrotreated naphtha having less than 0.5 ppmw sulfur and nitrogen, the process comprising:

separating a hydrotreated naphtha feedstream into an aromatic-rich stream and an aromatic-lean stream by contacting the feedstream with an extraction solvent and separating into an extract from which the aromatic-rich stream is obtained and a raffinate from which the aromatic-lean stream is obtained, wherein the aromatic-lean stream includes no more than 5 weight percent aromatic compounds and is characterized by a first N+2A value where N+2A is a sum of naphthenic compound compositional content and two times aromatic compositional content;

pre-reforming all or a portion of the aromatic-lean stream in the presence of hydrogen and an effective pre-reforming dehydrocyclization catalyst to produce a pre-reformed stream having decreased paraffinic content, and an increased naphthenic content and/or aromatic content, relative to the aromatic-lean stream, and wherein the pre-reformed stream has a second N+2A value that is greater than the first N+2A value;

catalytically reforming the pre-reformed stream to produce a reformate stream; and

separating all or a portion of the aromatic-rich stream in an aromatic complex for recovery of aromatic products.

8. The process as in claim 7 , further comprising separating a hydrotreated naphtha feedstream into a light naphtha stream and a heavy naphtha stream, wherein the light naphtha stream consists of at least 90 weight % C5-C6 hydrocarbons and wherein the heavy naphtha feedstream consists of at least 90 weight % C7-C11 or C7-C12 hydrocarbons, wherein the feedstream is all or a portion of the heavy naphtha stream, and wherein the light naphtha stream is subjected to pre-reforming together with or separate from all or a portion of the aromatic-lean stream.

9. The process as in claim 8 , wherein a temperature cut point between the light naphtha stream and the heavy naphtha stream is about 80-88° C.

10. The process as in claim 8 , wherein a temperature cut point between the light naphtha stream and the heavy naphtha stream is about 80° C.

11. The process as in claim 8 , wherein the light naphtha stream is subjected to pre-reforming together with all or a portion of the aromatic-lean stream.

12. The process as in claim 8 , wherein at least a portion of the reformate stream is passed to the aromatic complex together with all or a portion of the aromatic-rich stream for recovery of aromatic products.

13. The process as in claim 7 , wherein at least a portion of the reformate stream is passed to the aromatic complex together with all or a portion of the aromatic-rich stream for recovery of aromatic products.

14. The process as in claim 7 , wherein pre-reforming occurs at: a reaction temperature range of about 400-600° C.; a pressure of about 1-20 bars; an LHSV, on a fresh feed basis relative to the dehydrocyclization catalysts, of about 1-5 h −i ; and a hydrogen/hydrocarbon mole ratio of about 1-10.

15. The process as in claim 14 , wherein the pre-reforming dehydrocyclization catalyst comprises an active component carried on a support containing an inorganic oxide and a zeolitic component comprising an ultra-stable Y-type (USY) zeolite, and wherein the active component comprises a platinum group metal selected from the group consisting of ruthenium, rhodium, palladium, osmium, iridium and platinum.

16. The process as in claim 14 , wherein the pre-reforming dehydrocyclization catalyst comprises an active component carried on a support containing an inorganic oxide and zeolitic component comprising an ultra-stable Y-type (USY) zeolite in which a portion of aluminum atoms of the framework of said USY zeolite thereof is substituted with zirconium atoms and/or titanium and/or hafnium atoms forming a post-framework modified USY zeolite, wherein said post-framework modified USY zeolite contains from 0.1 to 5 mass % zirconium atoms and/or titanium and/or hafnium atoms as calculated as the oxide basis, and wherein the active component comprises a platinum group metal selected from the group consisting of ruthenium, rhodium, palladium, osmium, iridium and platinum.

17. The process as in claim 1 , wherein pre-reforming occurs at: a reaction temperature range of about 400-600° C.; a pressure of about 1-20 bars; an LHSV, on a fresh feed basis relative to the dehydrocyclization catalysts, of about 1-5 h −i ; and a hydrogen/hydrocarbon mole ratio of about 1-10.

18. The process as in claim 17 , wherein the pre-reforming dehydrocyclization catalyst comprises an active component carried on a support containing an inorganic oxide and a zeolitic component comprising an ultra-stable Y-type (USY) zeolite, and wherein the active component comprises a platinum group metal selected from the group consisting of ruthenium, rhodium, palladium, osmium, iridium and platinum.

19. The process as in claim 17 , wherein the pre-reforming dehydrocyclization catalyst comprises an active component carried on a support containing an inorganic oxide and zeolitic component comprising an ultra-stable Y-type (USY) zeolite in which a portion of aluminum atoms of the framework of said USY zeolite thereof is substituted with zirconium atoms and/or titanium and/or hafnium atoms forming a post-framework modified USY zeolite, wherein said post-framework modified USY zeolite contains from 0.1 to 5 mass % zirconium atoms and/or titanium and/or hafnium atoms as calculated as the oxide basis, and wherein the active component comprises a platinum group metal selected from the group consisting of ruthenium, rhodium, palladium, osmium, iridium and platinum.