CN106281434A

CN106281434A - A kind of method preparing lubricating oil for raw material with alhpa olefin

Info

Publication number: CN106281434A
Application number: CN201610654776.4A
Authority: CN
Inventors: 沈阳
Original assignee: Beijing Jie Hui Chemical Technology Co Ltd
Current assignee: Beijing Jie Hui Chemical Technology Co Ltd
Priority date: 2016-08-11
Filing date: 2016-08-11
Publication date: 2017-01-04

Abstract

The invention discloses a kind of method preparing lubricating oil for raw material with alhpa olefin, with alhpa olefin as raw material, it is added together with catalyst high-pressure reactor, it is passed through noble gas and gets rid of air, control inert gas pressure, at 5 ~ 200 DEG C, react 1 ~ 6h, prepare thick product, being then passed through membrane module and separate thick product and catalyst, isolated catalyst recycles, thick product alkali cleaning, wash, and distillation of reducing pressure obtains product with hydrotreating.The present invention, compared with conventional art, on the premise of meeting high-end product performance, expands raw material range, substitute or part substitutes 1 decene, reduce cost, and excellent product performance, do not use fluoride as catalytic component simultaneously, decrease the corrosion to the equipment of production and the pollution to environment.

Description

A kind of method preparing lubricating oil for raw material with alhpa olefin

Technical field

The invention belongs to petrochemical industry, be specifically related to a kind of method preparing lubricating oil for raw material with alhpa olefin.

Background technology

PAO is the abbreviation of English Polyalphaolefin, is the kind having the call in synthetic lubricant base oil, Having viscosity index (VI) high, pour point is low, the feature that evaporation loss is little, 1-decene the PAO excellent performance prepared, but raw material sources have Limit, expensive.

Summary of the invention

Goal of the invention: present invention aims to the deficiencies in the prior art, it is provided that one is prepared with alhpa olefin for raw material The method of lubricating oil.

Technical scheme: in order to reach foregoing invention purpose, the present invention is specifically performed by: one with alhpa olefin is The method of lubricating oil prepared by raw material, with alhpa olefin as raw material, it adds together with catalyst high-pressure reactor, is passed through indifferent gas Body gets rid of air, controls inert gas pressure, at 5 ~ 200 DEG C, reacts 1 ~ 6h, prepares thick product, be then passed through membrane module and divide From thick product and catalyst, isolated catalyst recycles, thick product alkali cleaning, washing, and reduce pressure distillation and hydrotreating Obtain product.

Wherein, described alhpa olefin is selected from 1-butylene, 1-hexene, 1-octene, 1-decene, 1-laurylene, 1-tetradecylene, 1-ten One or more in six alkene.

Wherein, described catalyst is made up of aluminum chloride and promoter 1000 ~ 50:1 in mass ratio, and promoter is selected from Water, methanol, ethanol, isopropanol, n-butyl alcohol, n-octyl alcohol, chloro-normal butane, tert-butyl chloride, triisobutyl aluminium, Ketohexamethylene, oneself Diketone.

Wherein, the addition of described catalyst is the 0.5 ~ 5% of alhpa olefin quality.

Wherein, described membrane module is to have the ceramic membrane of through hole, in order to separate thick product and catalyst.

Wherein, described noble gas is nitrogen, argon or helium, controls pressure in 0.5 ~ 1.5MPa.

Beneficial effect: the present invention is compared with conventional art, on the premise of meeting high-end product performance, expands raw material model Enclose, substitute 1-decene, reduce cost, and excellent product performance, do not use fluoride as catalytic component simultaneously, decrease To the corrosion of the equipment of production and the pollution to environment.

Detailed description of the invention

Embodiment 1:

Being 1 liter by internal volume, jacketed, the stainless steel autoclave of stirring carry out internal the most dried, add 1-own Alkene 300g, 1-decene 20 g, 1-laurylene 80 g.Add composite catalyst 8g, close autoclave, logical chuck cooling Water, logical nitrogen displaced air, and keep 0.1MPa nitrogen pressure.Open stirring, control the flow of cooling water, keep temperature in the kettle 10 ± 2 DEG C, open refrigeration machine if desired, keep cooling water temperature at 5 ± 2 DEG C.It is stirred at room temperature 2 hours, is cooled to room Temperature, in autoclave, mixture passes through membrane module, and isolated solid-phase catalyst uses as reaction cycle next time, the thick product of liquid phase Return autoclave, add the sodium hydrate aqueous solution 50g of 40%, continue stirring 0.5 hour, terminate reaction.

Product in autoclave is put in separatory funnel, separates and obtain upper organic phase, continue washing, until water The pH value of phase is 7.

Organic facies after washing is carried out decompression distillation, removes the boiling point light component less than 300 DEG C, obtain light yellow clear Liquid, 384g.

Product after distillation is put in the stainless steel autoclave of 1 liter, adds the hydrogenation catalyst that mass ratio is 1.5 %, React 7 hours in 120 DEG C under the hydrogen pressure of 2MPa.After reaction terminates, after temperature being cooled near 60 DEG C, take out and produce Thing, with the membrane module of 2 μm, filters separation at 60 DEG C by catalyst component, obtains hydride 386g.

Embodiment 2

With embodiment 1, difference is, 15 ± 2 DEG C of evidences of reaction temperature are shown in Table 1.

Embodiment 3

With embodiment 1, difference is, 20 ± 2 DEG C of evidences of reaction temperature are shown in Table 1.

Embodiment 4

With embodiment 1, difference is, 25 ± 2 DEG C of evidences of reaction temperature are shown in Table 1.

Embodiment 5

With embodiment 1, difference is, 30 ± 2 DEG C of evidences of reaction temperature are shown in Table 1.

Embodiment 6

With embodiment 1, difference is, reaction temperature 35 ± 2 DEG C.Data are shown in Table 1.

Embodiment 7

With embodiment 4, difference is, catalyst charge is 0.5%, and data are shown in Table 1.

Embodiment 8

With embodiment 4, difference is, catalyst charge is 1%, and data are shown in Table 1.

Embodiment 9

With embodiment 4, difference is, catalyst charge is 1.5%, and data are shown in Table 1.

Embodiment 10

With embodiment 4, difference is, catalyst charge is 2.5%, and data are shown in Table 1.

Embodiment 11

With embodiment 4, difference is, catalyst charge is 3%, and data are shown in Table 1.

Embodiment 12

With embodiment 4, difference is, catalyst charge is 3.5%, and data are shown in Table 1.

Embodiment 13

With embodiment 11, difference is, the response time is 1h, and data are shown in Table 1.

Embodiment 14

With embodiment 11, difference is, the response time is 3h, and data are shown in Table 1.

Embodiment 15

With embodiment 11, difference is, the response time is 4h, and data are shown in Table 1.

Embodiment 16

With embodiment 11, difference is, the response time is 5h, and data are shown in Table 1.

Embodiment 17

With embodiment 11, difference is, the response time is 6h, and data are shown in Table 1.

Embodiment 18

With embodiment 11, difference is, the response time is 7h, and data are shown in Table 1.

Embodiment 19

With embodiment 11, difference is, the response time is 8h, and data are shown in Table 1.

Embodiment 20

With embodiment 17, difference is, co-catalyst system and major catalyst mass ratio are 0.005, and data are shown in Table 1.

Embodiment 21

With embodiment 17, difference is, co-catalyst system and major catalyst mass ratio are 0.01, and data are shown in Table 1.

Embodiment 22

With embodiment 17, difference is, co-catalyst system and major catalyst mass ratio are 0.015, and data are shown in Table 1.

Embodiment 23

With embodiment 17, difference is, co-catalyst system and major catalyst mass ratio are 0.02, and data are shown in Table 1.

Embodiment 24

With embodiment 17, difference is, co-catalyst system and major catalyst mass ratio are 0.03, and data are shown in Table 1.

Claims

1. the method preparing lubricating oil for raw material with alhpa olefin, it is characterised in that with alhpa olefin as raw material, by itself and catalyst Add high-pressure reactor together, be passed through noble gas get rid of air, control inert gas pressure, at 5 ~ 200 DEG C, reaction 1 ~ 6h, prepares thick product, is then passed through membrane module and separates thick product and catalyst, and isolated catalyst recycles, thick product Alkali cleaning, washing, and distillation of reducing pressure.

The method preparing lubricating oil for raw material with alhpa olefin the most according to claim 1, it is characterised in that described alhpa olefin selects From 1-butylene, 1-hexene, 1-octene, 1-decene, 1-laurylene, 1-tetradecylene, one or more in 1-hexadecylene.

The method preparing lubricating oil for raw material with alhpa olefin the most according to claim 1, it is characterised in that described catalyst Be made up of aluminum chloride and promoter 1000 ~ 50:1 in mass ratio, promoter be selected from water, methanol, ethanol, isopropanol, just Butanol, n-octyl alcohol, chloro-normal butane, tert-butyl chloride, triisobutyl aluminium, Ketohexamethylene or acetyl butyryl.

The method preparing lubricating oil for raw material with alhpa olefin the most according to claim 1, it is characterised in that described catalyst Addition is alhpa olefin quality 0.5 ~ 5%.

The method preparing lubricating oil for raw material with alhpa olefin the most according to claim 1, it is characterised in that described membrane module For there is the ceramic membrane of through hole, in order to separate thick product and catalyst.

The method preparing lubricating oil for raw material with alhpa olefin the most according to claim 1, it is characterised in that described indifferent gas Body is nitrogen, argon or helium, controls pressure in 0.5 ~ 1.5MPa.