Catalytic dewaxing process

• US 4,917,789 A
• Filed: 02/03/1987
• Issued: 04/17/1990
• Est. Priority Date: 02/03/1987
• Status: Expired due to Term

• Current Assignee: Cosden Technology, Inc. (Totalenergies Se)
• Original Assignee: Fina Technology, Inc. (Totalenergies Se)
• Inventors: Butler, James R., Licht, William P.
• Primary Examiner(s): MCFARLANE, ANTHONY R
• Application Number:
  US07/010,224
• Time in Patent Office: 1,169 Days
• Field of Search: 208/111, 208/109, 208/89, 208/18, 208/15, 208/57, 208/118, 208/120
• US Class Current: 208/89
• CPC Class Codes: C10G 2300/70 Catalyst aspects
• CPC Class Codes: C10G 45/64 containing crystalline alumino-silicates, e.g. molecular sieves
• CPC Class Codes: C10G 65/043 at least one step being a change in the structural skeleton
• CPC Class Codes: F02B 3/06 with compression ignition compression ignition engines using air or gas for blowing fuel into compressed air in cylinder F02B13/02

Abstract

A process for reducing the pour point of sulfur containing gas oil fractions to produce fractions, including diesel oil of reduced pour point involving sequential hydrotreating and dewaxing of the gas oil feedstock. The hydrotreating step is carried out over a conventional hydrodesulfurization catalyst to remove sulfur. The dewaxing step is carried out over silicalite at mild dewaxing conditions under which the C₃ and lower gas make is no greater than 2 wt. % based upon the gas oil feed.

Claims

1. A process for catalytic dewaxing a hydrocarbon feed having an initial boiling point of less than 500°

F. and a final boiling point of less than 900°

F., comprising passing the hydrocarbon feed through a reaction zone containing a crystalline silica polymorph silicalite catalyst at mild dewaxing conditions under which the C₃ and lower hydrocarbon gas make from said reaction zone is not greater than 2 wt. % based on the feed.

2. The process of claim 1 wherein the C₃ and lower hydrocarbon gas make from said reaction zone is no greater than 1 wt. % based upon said feed.

3. A process for catalytically dewaxing a hydrocarbon feed having an initial boiling point of less than 500°

F. and a final boiling point of less than 900°

F., comprising passing the hydrocarbon feed through a reaction zone containing a crystalline silica polymorph silicalite catalyst at mild dewaxing conditions under which the liquid yield from said reaction zone is greater than 100% by volume based on the feed.

4. A process for reducing the pour point of a sulfur containing gas oil boiling in the range of 400°

-900°

F. comprising the steps of;

(a) catalytically hydrotreating said gas oil to remove sulfur therein; and

(b) dewaxing said gas oil by passing said gas oil over a crystalline silica polymorph silicalite catalyst at mild dewaxing conditions under which the total C₃ and lower hydrocarbon gas make is no greater than 2 wt. % based on said gas oil feed.

5. The process of claim 4 wherein said hydrotreating step is carried out initially and the effluent from said hydrotreating step is then subjected to said dewaxing step.

6. The process of claim 5 wherein said dewaxing step is carried out at a higher temperature than said hydrotreating step.

7. The process of claim 4 wherein the said dewaxing step is carried out initially and the effluent from said dewaxing step is passed to said hydrotreating step.

8. The process of claim 4 wherein step (b) is carried out at a space velocity greater than the space velocity of step (a).

9. In the dewaxing of hydrocarbons to provide a diesel oil fraction of reduced pour point, the method comprising:

(a) feeding hydrocarbon fraction having an initial boiling point of less than 500°

F. and a final boiling point of less than 900°

F. into a first reaction zone operated at a temperature within the range of 550°

-800°

F. and a pressure of at least 300 psia and within first reaction zone catalytically hydrotreating said fraction to remove sulfur therefrom;

(b) passing the hydrotreated hydrocarbon fraction from said first reaction zone to a second reaction zone under operating conditions including a temperature within the range of 650°

-850°

F. to limit the amount of C₁ -C₃ hydrocarbons produced by cracking of said fraction to no more than 2 wt. % of the feed in step (a) and within said second zone dewaxing said fraction over a silicalite dewaxing catalyst to provide a product having a lower pour point than said feed; and

(c) withdrawing a diesel oil product from said second reaction zone.

10. The process of claim 9 wherein said diesel oil product has a final boiling point in excess of 670°

F.

11. The process of claim 9 wherein said diesel oil product has a final boiling point of at least 680°

F.

12. The process of claim 9 wherein said first and second reaction zones are in separate reactors.

13. The process of claim 12 wherein the reactor for said second reaction zone is operated at a higher temperature than the reactor for said first reaction zone.

14. The process of claim 13 wherein the incremental difference between the inlet temperature to said first reaction zone and the inlet temperature in said second reaction zone is at least 50°

F.

15. The process of claim 12 wherein the reaction zone temperatures in said first and second reactors are controlled independently of one another.

16. The process of claim 9 wherein the average boiling point of the 50-100% volume boiling fraction of the product effluent from said second reaction zone is reduced by an average of no more than 30°

F. from the 50-100% boiling fraction of the hydrocarbon fraction fed to said first reaction zone.

17. The process of claim 9 wherein step (b) is carried out at a space velocity greater than the space velocity of step (a).