Method of making high energy distillate fuels

• US 9,127,217 B2
• Filed: 12/18/2008
• Issued: 09/08/2015
• Est. Priority Date: 12/21/2007
• Status: Active Grant

• Current Assignee: Chevron USA Incorporated (Chevron Corp.)
• Original Assignee: Chevron USA Incorporated (Chevron Corp.)
• Inventors: Lopez, Jaime, Lichtenberger, Janine
• Primary Examiner(s): Robinson, Renee E
• Application Number:
  US12/338,388
• Publication Number:
  US 20090159489A1
• Time in Patent Office: 2,455 Days
• Field of Search: 208/15, 208/58, 208/60, 208/89
• US Class Current: 1/1
• CPC Class Codes: C10G 2300/1048 Middle distillates
• CPC Class Codes: C10G 2300/1096 Aromatics or polyaromatics
• CPC Class Codes: C10G 2300/202 Heteroatoms content, i.e. S, N, O, P
• CPC Class Codes: C10G 2300/308 Gravity, density, e.g. API
• CPC Class Codes: C10G 2400/04 Diesel oil
• CPC Class Codes: C10G 2400/08 Jet fuel
• CPC Class Codes: C10G 45/50 in combination with chromium, molybdenum or tungsten metal, or compounds thereof
• CPC Class Codes: C10G 47/20 the catalyst containing other metals or compounds thereof
• CPC Class Codes: C10G 65/043 at least one step being a change in the structural skeleton
• CPC Class Codes: C10G 65/08 at least one step being a hydrogenation of the aromatic hydrocarbons
• CPC Class Codes: C10G 65/12 including cracking steps and other hydrotreatment steps

Abstract

A process of upgrading a highly aromatic hydrocarbon feedstream comprising

(a) contacting a highly aromatic hydrocarbon feedstream, having a normal paraffin content of greater than at least about 5 wt %, wherein a major portion of the feedstream has a boiling range of from about 300° F. to about 800° F. under catalytic conditions with a catalyst system, containing a hydrotreating catalyst, a hydrogenation/hydrocracking catalyst, and a dewaxing catalyst in a single stage reactor system, wherein the active metals in the hydrogenation/hydrocracking catalyst comprises from about 5%-30% by weight of nickel and from about 5%-30% by weight tungsten; and
(b) wherein at least a portion of the highly aromatic hydrocarbon feedstream is converted to a product stream having a boiling range within jet or diesel boiling ranges.

Claims

1. A process of upgrading a highly aromatic hydrocarbon feedstream to a product stream having a boiling range within a jet boiling range, the process comprising:

(a) contacting a highly aromatic hydrocarbon feedstream, having a normal paraffin content of greater than at least about 5 wt %, wherein a major portion of the feedstream has a boiling range of from about 300°

F. to about 800°

F. and wherein the feedstream has an aromatic content of at least 40 wt % and a sulfur content up to 3 wt %, under catalytic conditions with a catalyst system, containing a hydrotreating catalyst, a hydrogenation/hydrocracking catalyst, and non-Group VIB or Group VIII metal hydrogenation component-containing zeolitic dewaxing catalyst in a single stage reactor system, wherein the active metals in the hydrogenation/hydrocracking catalyst comprises from about 20%-30% by weight of nickel and from about 5%-30% by weight tungsten;

wherein the single stage reactor system comprises a hydrotreating section and a hydrocracking section and further wherein the hydrocracking section comprises the hydrocracking catalyst and the dewaxing catalyst, wherein the dewaxing catalyst is layered with the hydrocracking catalyst or the dewaxing catalyst is blended with the hydrocracking catalyst; and

(b) wherein at least a portion of said highly aromatic hydrocarbon feedstream is converted to the product stream having a boiling range within the jet boiling range, and further wherein the product stream has a net heat of combustion of greater than 125.000 Btu/gal and an aromatic saturation that is greater than 70 wt. %.

2. The process according to claim 1 wherein the active metals in the hydrogenation/hydrocracking catalyst consists essentially of from about 20%-30% by weight of nickel and from about 5%-30% by weight tungsten.

3. The process according to claim 1 wherein the hydrocracking section comprises no more than 30 wt of the dewaxing catalyst.

4. The process according to claim 1 wherein the hydrocracking section comprises at least one reactor bed.

5. The process according to claim 1 wherein the product stream is separated into a jet fuel product.

6. The process according to claim 1 wherein said major portion of the feedstream has a boiling range of from about 300°

F. to about 600°

F.

7. The process according to claim 1, wherein the feedstream has an aromatic content of at least 40 wt % up to about 80 wt %.

8. The process according to claim 1 wherein the zeolitic dewaxing catalyst is a crystalline aluminosilicate zeolite dewaxing catalyst.

9. The process according to claim 8 wherein the crystalline aluminosilicate zeolite dewaxing catalyst is ZSM-5.