# US 2013/0158314 A1 · Saturation process for making lubricant base oils > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 2013/0158314 A1 - Document ID: US20130158314A1 - Status: Published application - Kind: A1 - Application number: 13/687,379 - Filed: 2012-11-28 - Published: 2013-06-20 - Earliest claimed: 2011-12-15 - Assignees: ExxonMobil Research and Engineering Company - Inventors: Gary Paul Schleicher; Jason Thomas Calla - Web page: https://patentgrep.com/patent/US20130158314A1 ## CPC - C10G 65/02: plural serial stages only - C10G 51/02: plural serial stages only - C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES ## Abstract Systems and methods are provided for hydroprocessing a petroleum fraction, such as a bottoms fraction from a fuels hydrocracking process, to generate a lubricant base oil. A fuels hydrocracking process typically has less stringent requirements for the sulfur and nitrogen content of a feed as compared to a lubricant base oil. Additionally, depending on the nature of the feed for the fuels hydrocracking process, the bottoms fraction may contain a relatively high level of aromatics compounds. The aromatic content of such a petroleum fraction can be reduced using a aromatic saturation stage with multiple catalyst beds, or alternatively using a reactor (or reactors) with multiple aromatic saturation stages. The catalysts in the various beds or stages can be selected to provide different types of aromatic saturation activity. An initial bed or stage can provide activity for saturation of 1-ring aromatics in the petroleum fraction. One or more subsequent beds or stages, operating at successively lower temperature, can then be used to reduce the multiple-ring aromatic content of the petroleum fraction. ## Claims ### Claim 1 A method for producing a lubricant base oil, comprising: contacting an input feed having an aromatics content of at least 600 mmol/kg with a first catalyst under first effective aromatic saturation conditions to produce a first effluent containing less than 600 mmol/kg of aromatics, the first effective aromatic saturation conditions including a temperature of at least 300° C.; contacting the first effluent with a second catalyst under second effective aromatic saturation conditions to produce a second effluent, the second effective aromatic saturation conditions including a temperature of from 270° C. to 300° C. and a hydrogen partial pressure of at least 4.1 MPag (600 psig); and contacting the second effluent with a third catalyst under third effective aromatic saturation conditions, the third effective aromatic saturation conditions including a temperature of from 220° C. to 260° C. ### Claim 2 (depends on 1) The method of claim 1, wherein the first catalyst comprises a dewaxing catalyst that operates primarily by isomerization. ### Claim 3 A method for producing a lubricant base oil, comprising: hydrocracking a feedstock having a T5 boiling point of at least 550° C. under effective hydrocracking conditions to form a hydrocracked feedstock having an aromatics content of at least 200 mmol/kg; fractionating the hydrocracked feedstock to form at least a diesel fraction and a fraction having a higher boiling range than the diesel fraction; contacting the higher boiling range fraction with a dewaxing catalyst that operates primarily by isomerization under first effective aromatic saturation conditions to produce a first effluent containing a lower amount of aromatic than the hydrocracked feedstock, the first effective aromatic saturation conditions including a temperature of at last 300° C.; contacting the first effluent with a second catalyst under second effective aromatic saturation conditions to produce a second effluent, the second effective aromatic saturation conditions including a temperature of from 270° C. to 300° C. and a hydrogen partial pressure of at least 4.1 MPag (600 psig); and contacting the second effluent with a third catalyst under third effective aromatic saturation conditions, the third effective aromatic saturation conditions including a temperature of from 220° C. to 260° C. ### Claim 4 (depends on 1, 3) The method of claims 1 or 3, wherein the first catalyst comprises ZSM-48, ZSM-23, or a combination of ZSM-48 and ZSM-23, a binder, and from 0.1 wt % to 1.5 wt % of Pt supported on the catalyst. ### Claim 5 (depends on 1, 3) The method of claims 1 or 3, wherein the second catalyst comprises MCM-41, ZSM-48, ZSM-23, or a combination of ZSM-48 and ZSM-23, a binder, and from 0.1 wt % to 1.5 wt % of Pt, Pd, or a combination of Pt and Pd. ### Claim 6 (depends on 1, 3) The method of claims 1 or 3, wherein the third catalyst comprises MCM-41, a binder, and from 0.1 wt % to 1.5 wt % of Pt, Pd, or a combination of Pt and Pd. ### Claim 7 A method for producing a lubricant base oil, comprising: contacting an input feed having an aromatics content of at least 200 mmol/kg, and a mutagenicity index of at least 1.0 with a first catalyst under first effective aromatic saturation conditions to produce a first effluent containing a lower amount of aromatics than the input feed prior to contacting, the first catalyst comprising from 0.1 wt % to 1.5 wt % Pt on a support including a binder and ZSM-48, ZSM-23, or a combination of ZSM-48 and ZSM-23, the first effective aromatic saturation conditions including a temperature of at last 300° C.; contacting the first effluent with a second catalyst under second effective aromatic saturation conditions to produce a second effluent, the second catalyst comprising from 0.1 to 1.5 wt % of a metal selected from Pt, Pd, or a combination of Pt and Pd, a binder, and MCM-41, ZSM-48, ZSM-23, or a combination of ZSM-48 and ZSM-23, the second effective aromatic saturation conditions including a temperature of from 270° C. to 300° C. and a hydrogen partial pressure of at least 2.4 MPag (400 psig); and contacting the second effluent with a third catalyst under third effective aromatic saturation conditions, the third catalyst comprising from 0.1 to 1.5 wt % of a metal selected from Pt, Pd, or a combination of Pt and Pd, a binder, and MCM-41, the third effective aromatic saturation conditions including a temperature of from 220° C. to 260° C. ### Claim 8 (depends on 7) The method claim 7, wherein the first catalyst and the second catalyst are the same. ### Claim 9 (depends on 7) The method of claims 7, wherein the input feed comprises at least 2000 mmol/kg of aromatics. ### Claim 10 (depends on 7) The method of claim 7, wherein the second effective aromatic saturation conditions include a hydrogen partial pressure of at least 5.2 MPag (750 psig). ### Claim 11 (depends on 7) The method of claim 7, further comprising quenching the first effluent using a gas phase quench stream containing hydrogen. ### Claim 12 (depends on 7) The method of claim 7, wherein the second catalyst and the third catalyst are the same.