Base oil manufacturing plant

Patent metadata

Field	Value
Publication number	US-8956581-B2
Application number	US-201314031334-A
Country	US
Kind code	B2
Filing date	Sep 19, 2013
Priority date	Oct 1, 2008
Publication date	Feb 17, 2015
Grant date	Feb 17, 2015

Abstract

We provide a process to manufacture a base stock, comprising hydrocracking, separating, and dewaxing, wherein the base stock has a ratio of Noack volatility to CCS VIS at −25° C. multiplied by 100 from 0.15 to 0.40. We also provide a base stock made by a process, and a base oil manufacturing plant that produces the base stock.

First claim

We claim:

1. A base oil manufacturing plant, comprising:
a hydrocracking reactor comprising a product slate containing greater than 20 wt % of a waxy intermediate fraction,
a first conduit from the hydrocracking reactor to a vacuum distillation tower, and
a second conduit from the vacuum distillation tower to a hydroisomerization dewaxing reactor, wherein the hydroisomerization dewaxing reactor comprises a first base stock having:
i. a first boiling range from 730 to 1000° F. (388 to 538° C.),
ii. a first VI from 105 to 120,
iii. a first CCS VIS at −25° C. from 2500 to 4500 mPa·s, and
iv. a ratio of a first Noack volatility to the first CCS VIS at −25° C. multiplied by 100 from 0.15 to 0.40.

2. The base oil manufacturing plant of claim 1 , further comprising a third conduit from the vacuum distillation tower to the hydroisomerization dewaxing reactor, wherein the hydroisomerization dewaxing reactor further comprises an additional base stock having:
a. an additional boiling range from 700 to 925° F. (371 to 496° C.),
b. an additional VI from 105 to 119, and
c. an additional Noack volatility less than 18 wt %.

3. The base oil manufacturing plant of claim 1 , wherein the vacuum distillation tower comprises a higher boiling fraction of the waxy intermediate fraction that is block dewaxed in the hydroisomerization dewaxing reactor to produce the first base stock.

4. The base oil manufacturing plant of claim 1 , wherein the vacuum distillation tower follows the hydrocracking reactor.

5. The base oil manufacturing plant of claim 1 , wherein the vacuum distillation tower comprises a lower boiling fraction of the waxy intermediate fraction that is block dewaxed in the hydroisomerization dewaxing reactor to produce the additional base stock.

6. The base oil manufacturing plant of claim 2 , wherein the additional base stock has a ratio of the additional Noack volatility to an additional CCS VIS at −25° C. from 0.80 to 1.55.

7. The base oil manufacturing plant of claim 1 , wherein the first base stock has a ratio of the first Noack volatility to the first CCS VIS at −25° C. multiplied by 100 from 0.20 to 0.35.

8. The base oil manufacturing plant of claim 2 , wherein the first base stock and the additional base stock are Group II base oils.

9. The base oil manufacturing plant of claim 1 , additionally comprising a hydrofinishing reactor.

10. The base oil manufacturing plant of claim 1 , wherein the hydroisomerization dewaxing reactor comprises a catalyst having a shape selective intermediate pore size molecular sieve selected from the group consisting of SAPO-11, SAPO-31, SAPO-41, SM-3, SM-7, ZSM-22, ZSM-23, ZSM-35, ZSM-48, ZSM-57, SSZ-32, SSZ-32X, metal modified SSZ-32X, offretite, ferrierite, and combinations thereof.

Assignees

• Rosenbaum John Michael
• Lok Brent K
• Helling Kathy A
• Lee Stephen K
• Chevron Usa Inc

Inventors

• Rosenbaum John Michael
• Lok Brent K
• Helling Kathy A
• Lee Stephen K
• Schexnaydre Ryan Joseph

Classifications

• B01D3/009

  in combination with chemical reactions · CPC title

• C10G67/04

  including solvent extraction as the refining step in the absence of hydrogen · CPC title

• C10M2203/003

  used as base material · CPC title

• C10G65/12 Primary

  including cracking steps and other hydrotreatment steps · CPC title

• C10N2030/74

  Noack Volatility · CPC title