润滑科技信息平台

机械工程学会摩擦学分会固体润滑国家重点实验室摩擦学学报

使用二氢左旋葡萄糖酮作为溶剂,通过逆流液液萃取去除润滑油原料中的芳香族和极性化合物

专利摘要

一种方法可包括:将包含真空瓦斯油的流引入液-液萃取单元; 使减压瓦斯油与二氢左旋葡萄糖烯酮溶剂接触,以从减压瓦斯油中萃取一部分芳香族化合物,从而产生具有降低的芳香族化合物浓度的萃余物流; 并对萃余液流进行脱蜡以形成基础油。 ......

基本信息

专利类型:
发明专利
申请/专利号:
PCT/US2024/016512
申请日期:
2024-02-20
专利申请人:
埃克森美孚科技工程公司
分类号:
["C10G9/00","C10G45/32","C10G45/44","C10G67/04","C10G67/14","C10G69/06"]
发明/设计人:
ARIDI, TOUFIC ， SINCLAIR, DARDEN STEVE ， PHILLIPS, GAITHER M. ， WHEELER, CHRISTOPHER J.
权利要求: CLAIMS:1. A method comprising: introducing a stream comprising a vacuum gas oil into a liquid-liquid extraction unit; contacting the vacuum gas oil with a dihydrolevoglucosenone solvent to extract a portion of aromatic compounds from the vacuum gas oil to produce a raffinate stream with reduced aromatic compound concentration; and dewaxing the raffinate stream to form a base stock.2. The method of claim 1 wherein the vacuum gas oil has a T5 boiling point of at least about 371 °C and a T95 boiling point of about 538 °C or less.3. The method of any of claims 1-2 wherein the dihydrolevoglucosenone solvent comprises dihydrolevoglucosenone and water wherein the water is present in an amount of 0.1 vol.% to 10 vol.% of the dihydrolevoglucosenone solvent.4. The method of any of claims 1-3 wherein the dihydrolevoglucosenone solvent is introduced into the liquid-liquid extraction unit in an amount of about 100 vol.% to about 300 vol. % of the deasphalted oil.5. The method of any of claims 1-4 wherein the dihydrolevoglucosenone solvent is introduced into the liquid-liquid extraction unit at a temperature at least about 10 °C to about 20 °C higher than the deasphalted oil.6. The method of any of claims 1-5 wherein the base stock has a viscosity index in a range of about 80 to about 120 as measured by ASTM D2270-93.7. The method of any of claims 1-6 wherein the base stock has a kinematic viscosity at 100 °C (KV100) at a point in a range of about 13 cSt to about 16.5 cSt as measured by ASTM D 445-01.8. The method of any of claims 1-7 wherein the base stock has a kinematic viscosity at 40 °C (KV40) at a point in a range of about 135 cSt to about 200 cSt as measured by ASTM D 445-01.9. The method of any of claims 1-8 wherein the dewaxing comprises solvent dewaxing and wherein the base stock is a Group I base stock.10. The method of any of claims 1-9 wherein the dewaxing comprises catalytic dewaxing and wherein the base stock is a Group II or a Group III base stock.11. A method comprising: thermally cracking a hydrocarbon feedstock to produce a cracked product stream; separating at least a portion of the cracked product stream to form a lubricant boiling range fraction of the cracked product stream; deasphalting at least a portion of the lubricant boiling range fraction to form a deasphalted oil; introducing the deasphalted oil into a liquid-liquid extraction unit; contacting the deasphalted oil with a dihydrolevoglucosenone solvent to extract a portion of aromatic compounds from the deasphalted oil to produce a raffinate stream with reduced aromatic compound concentration; and dewaxing the raffinate stream to form a base stock.12. The method of claim 11 wherein thermally cracking the hydrocarbon feedstock comprises at least one process selected from the group consisting of fluidized coking, delayed coking, hydroconversion, and combinations thereof.13. The method of any of claims 11-12 wherein the lubricant boiling range fraction has a 10% distillation boiling point of 343 °C - 370 °C.14. The method of any of claims 11-13 wherein the liquid-liquid extraction unit comprises a counter-current liquid-liquid extractor.15. The method of any of claims 11-14 wherein the dihydrolevoglucosenone solvent comprises dihydrolevoglucosenone and water wherein the water is present in an amount of 0.1 vol.% to 10 vol.% of the dihydrolevoglucosenone solvent.16. The method of any of claims 11-15 wherein the dihydrolevoglucosenone solvent is introduced into the liquid-liquid extraction unit in an amount of about 100 vol.% to about 300 vol. % of the deasphalted oil.17. The method of any of claims 11-16 wherein the dihydrolevoglucosenone solvent is introduced into the liquid-liquid extraction unit at a temperature at least about 10 °C to about 20 °C higher than the deasphalted oil.18. The method of any of claims 11-17 wherein the dewaxing comprises solvent dewaxing and wherein the base stock is a Group I base stock.19. The method of any of claims 11-18 wherein the dewaxing comprises catalytic dewaxing and wherein the base stock is a Group II or a Group III base stock.20. The method of any of claims 11-19 wherein the base stock has a kinematic viscosity at 100 °C (KV100) at a point in a range of about 13 cSt to about 16.5 cSt as measured by ASTM D 445-01.21. The method of any of claims 11-20 wherein the base stock has a kinematic viscosity at 40 °C (KV40) at a point in a range of about 135 cSt to about 200 cSt as measured by ASTM D 445-01.22. The method of any of claims 11-21 wherein the base stock wherein the base stock has a viscosity index in a range of about 80 to about 120 as measured by ASTM D2270-93.23. The method of any of claims 11-22 wherein the base stock has a pour point at a point in a range of 0° C to -25° C as measured by ASTM D97.24. The method of any of claims 11-23 further comprising hydrotreating the raffinate stream prior to dewaxing the raffinate stream.