CN109423351B - Low-temperature switch oil and preparation method thereof - Google Patents

Low-temperature switch oil and preparation method thereof Download PDF

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CN109423351B
CN109423351B CN201710727240.5A CN201710727240A CN109423351B CN 109423351 B CN109423351 B CN 109423351B CN 201710727240 A CN201710727240 A CN 201710727240A CN 109423351 B CN109423351 B CN 109423351B
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oil
low
temperature switch
temperature
catalyst
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CN109423351A (en
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柯友胜
马蕊燕
张静
何军
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Petrochina Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M101/00—Lubricating compositions characterised by the base-material being a mineral or fatty oil
    • C10M101/02—Petroleum fractions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M101/00—Lubricating compositions characterised by the base-material being a mineral or fatty oil
    • C10M101/02—Petroleum fractions
    • C10M101/025—Petroleum fractions waxes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M169/00—Lubricating compositions characterised by containing as components a mixture of at least two types of ingredient selected from base-materials, thickeners or additives, covered by the preceding groups, each of these compounds being essential
    • C10M169/04—Mixtures of base-materials and additives
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2203/00—Organic non-macromolecular hydrocarbon compounds and hydrocarbon fractions as ingredients in lubricant compositions
    • C10M2203/10—Petroleum or coal fractions, e.g. tars, solvents, bitumen
    • C10M2203/106—Naphthenic fractions
    • C10M2203/1065—Naphthenic fractions used as base material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2205/00—Organic macromolecular hydrocarbon compounds or fractions, whether or not modified by oxidation as ingredients in lubricant compositions
    • C10M2205/16—Paraffin waxes; Petrolatum, e.g. slack wax
    • C10M2205/163—Paraffin waxes; Petrolatum, e.g. slack wax used as base material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2207/00—Organic non-macromolecular hydrocarbon compounds containing hydrogen, carbon and oxygen as ingredients in lubricant compositions
    • C10M2207/02—Hydroxy compounds
    • C10M2207/023—Hydroxy compounds having hydroxy groups bound to carbon atoms of six-membered aromatic rings
    • C10M2207/026—Hydroxy compounds having hydroxy groups bound to carbon atoms of six-membered aromatic rings with tertiary alkyl groups
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2030/00—Specified physical or chemical properties which is improved by the additive characterising the lubricating composition, e.g. multifunctional additives
    • C10N2030/02—Pour-point; Viscosity index
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2030/00—Specified physical or chemical properties which is improved by the additive characterising the lubricating composition, e.g. multifunctional additives
    • C10N2030/10—Inhibition of oxidation, e.g. anti-oxidants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10N2030/00—Specified physical or chemical properties which is improved by the additive characterising the lubricating composition, e.g. multifunctional additives
    • C10N2030/64—Environmental friendly compositions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2040/00—Specified use or application for which the lubricating composition is intended
    • C10N2040/14—Electric or magnetic purposes
    • C10N2040/16—Dielectric; Insulating oil or insulators

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  • General Chemical & Material Sciences (AREA)
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Abstract

The invention provides low-temperature switch oil and a preparation method thereof, wherein the low-temperature switch oil comprises the following components: the low-temperature switch base oil comprises low-temperature switch base oil and a phenol antioxidant, wherein the weight of the phenol antioxidant accounts for 0.1-0.4% of that of the low-temperature switch base oil; the low-temperature switch base oil is prepared by the following method: and catalytically hydrogenating the naphthenic base crude oil and/or the paraffin base crude oil to generate crude oil, and collecting the fraction of the crude oil at the temperature of 220-290 ℃, wherein the fraction is the low-temperature switch base oil. The low-temperature switching oil disclosed by the invention has the advantages of smaller kinematic viscosity at high and low temperatures, excellent oxidation stability, small oil product carbonization tendency, low pour point, suitability for low-temperature environments, better solubility for oil sludge generated by oil product degradation and accordance with the environmental protection requirement.

Description

Low-temperature switch oil and preparation method thereof
Technical Field
The invention relates to an insulating oil technology for power equipment, in particular to low-temperature switch oil and a preparation method thereof, and belongs to the technical field of power equipment.
Background
The transformer oil switch is also called high-voltage breaker, is an important electrical equipment in a transformer device, and mainly has the main functions of cutting off or switching on a circuit with load and automatically cutting off short-circuit current when short circuit occurs. When a circuit with current is cut off, a moving contact and a static contact in the transformer oil switch are separated, electric arcs are generated between gaps of the static contact and the moving contact, the temperature of the electric arcs can reach over thousands of degrees centigrade, and high temperature can cause damage to a conductive part and an insulator, so that safe operation of electrical equipment is threatened. Therefore, the high-voltage switch is required to rapidly extinguish electric arcs in a small closed container, and the basic types of arc extinguishing modes in the closed container are that firstly, media such as sulfur hexafluoride, vacuum and oil are adopted; secondly, rapidly leading out energy from the electric arc by adopting air blowing, magnetic blowing and other modes; and thirdly, rapidly lengthening the arc, etc. Mineral petroleum products are used as arc extinguishing media, and are called switching oil, namely high-voltage switching oil. The high-voltage switch for filling oil is generally called high-voltage oil switch. The working principle is that the switch oil is decomposed and gasified at high temperature of the electric arc, and hydrogen in the decomposed gas has excellent heat conductivity and insulating strength, so that the arc injection temperature can be quickly reduced, and the insulating strength between electrodes can be improved. This feature is very beneficial for arc quenching and can serve to quench the arc. The switch oil medium is economical in a plurality of switch arc-extinguishing media, has the characteristic of rich use experience, and has a certain proportion when being applied to medium and high voltage switches.
At present, domestic electrical switching oil is less and has the defects of environmental pollution and high pour point, which are not suitable for being used in cold climatic regions, so mineral transformer oil is often used to replace the electrical switching oil, but the mineral transformer oil has the problems of poor arc extinguishing effect and serious oil carbonization tendency in the using process.
Disclosure of Invention
Aiming at the defects, the invention provides the low-temperature switching oil and the preparation method thereof, the low-temperature switching oil has smaller kinematic viscosity at high and low temperatures, excellent oxidation stability, small oil product carbonization tendency, low pour point, suitability for low-temperature environment, better solubility for oil sludge generated by oil product degradation, and meets the requirement of environmental protection.
The invention provides low-temperature switch oil which comprises the following components: the low-temperature switch base oil comprises low-temperature switch base oil and a phenol antioxidant, wherein the weight of the phenol antioxidant accounts for 0.1-0.4% of that of the low-temperature switch base oil;
the low-temperature switch base oil is prepared by the following method: and catalytically hydrogenating the naphthenic base crude oil and/or the paraffin base crude oil to generate crude oil, and collecting the fraction of the crude oil at the temperature of 220-290 ℃, wherein the fraction is the low-temperature switch base oil.
The low-temperature switching oil comprises low-temperature switching base oil and a phenol antioxidant, wherein the low-temperature switching base oil is a main component. The low-temperature switch base oil is prepared by taking naphthenic base crude oil and/or paraffin base crude oil as raw materials and combining catalytic hydrogenation and distillation processes, wherein the catalytic hydrogenation process can adjust and change the molecular structure of the low-temperature switch base oil, so that sulfur, nitrogen, colloid, asphaltene and the like of the low-temperature switch base oil are removed, and the viscosity-temperature performance and the anti-oxidation stability performance of the low-temperature switch base oil are improved.
When the preparation raw material of the low-temperature switch base oil of the present invention is a mixture of naphthenic base crude oil and paraffin base crude oil, the present invention does not limit the mass ratio between the naphthenic base crude oil and the paraffin base crude oil. Meanwhile, in the present invention, the phenolic antioxidant is preferably 2, 6-di-t-butyl-p-cresol.
According to the low-temperature switch oil provided by the invention, the aromatic hydrocarbon content in the low-temperature switch oil is 1-3%, the naphthenic hydrocarbon content in the low-temperature switch oil is 60-84%, the paraffin hydrocarbon content in the low-temperature switch oil is 15-30%, and the pour point of the low-temperature switch oil is less than-70 ℃. In addition, the low-temperature switch oil disclosed by the invention also meets various index requirements of the low-temperature switch oil in the standard GB 2536-2011. The low-temperature switching oil has high naphthene content, so that the low-temperature switching oil has excellent dissolving performance, can dissolve free carbon particles generated in the operation process of equipment, can promote oil to be rapidly decomposed into gas under the action of high-temperature electric arcs when the switching equipment acts, is extremely favorable for arc extinction, has a pour point which is 28-30 ℃ lower than that of the conventional low-temperature switching oil product, and can be widely used in a low-temperature environment. Meanwhile, the low-temperature switch oil has good oxidation stability and meets the requirement of environmental protection.
The invention also provides a preparation method of any one of the low-temperature switch oil, which comprises the following steps:
1) catalytically hydrogenating the naphthenic base crude oil and/or paraffin base crude oil to generate crude oil;
2) subjecting the crude oil to a first distillation and collecting a fraction at 150-;
3) performing second distillation on the fraction at the temperature of 150-350 ℃ in the step 2), and collecting a fraction at the temperature of 220-290 ℃, wherein the fraction at the temperature of 220-290 ℃ is the low-temperature switch base oil;
4) adding the phenol antioxidant into the low-temperature switch base oil to prepare the low-temperature switch oil; wherein the weight of the phenolic antioxidant accounts for 0.1-0.4% of the weight of the low-temperature switch base oil.
In the preparation method, the steps 1) -3) are used for preparing the low-temperature switch base oil, wherein the step 1) is used for carrying out catalytic hydrogenation on the raw material to produce the crude oil, the steps 2) -3) are used for distilling the crude oil produced in the step 1), and the crude oil is distilled twice in order to obtain the fraction of the crude oil with higher purity at the temperature of 220-. Wherein, the first distillation can collect the fraction at the temperature of 150-350 ℃ by performing the operation of ordinary reduced pressure (the operation pressure is 7.9KPa) distillation, the second distillation is the distillation (the operation pressure is 0.8KPa) which is carried out by taking the fraction (the fraction at the temperature of 150-350 ℃) of the first distillation as the mixture to be distilled and collects the fraction at the temperature of 220-290 ℃, and the fraction collected by the second distillation is the low-temperature switch base oil.
And then, heating the low-temperature switch base oil to 50-70 ℃, and adding a phenolic antioxidant, preferably 2, 6-di-tert-butyl-p-cresol, to prepare the low-temperature switch oil. Wherein the weight of the phenolic antioxidant is 0.1-0.4% of that of the low-temperature switch base oil.
The step 1) specifically comprises the step of introducing the naphthenic base crude oil and/or the paraffin base crude oil into a hydrogenation fixed bed reactor filled with a catalyst, wherein the volume ratio of hydrogen to the naphthenic base crude oil and/or the paraffin base crude oil is (400-1200): 1, controlling the reaction temperature of the catalytic hydrogenation to be 200-400 ℃, the hydrogen partial pressure to be 10-20MPa, and the liquid volume space velocity to be 0.3-2.0/h. Under the condition of hydrogen and catalyst, the naphthenic base crude oil and/or paraffin base crude oil can complete hydrogenation reaction. The present invention is not limited to the reaction site or the reaction vessel, and any vessel capable of satisfying the catalytic hydrogenation reaction except the fixed bed reactor for hydrogenation may be used for the above reaction.
Further, the catalyst adopted by the invention is a mixture, and comprises the following components in percentage by weight: 3-18% of nickel oxide, 3-10% of molybdenum oxide, 1-4% of cobalt oxide, 3-8% of tungsten oxide and the balance of silicon oxide. Wherein the silicon oxide is a carrier for other oxides. At the same time, the invention also limits the physical properties of the catalystSo as to ensure good catalytic conditions, in particular a catalyst having an average pore diameter of
Figure BDA0001385380970000031
The average pore volume is 0.1-2.0cm3(g) average specific surface area of 100-3G, strength of 20-100N/mm.
In order to improve the catalytic efficiency, the catalyst may be subjected to a sulfiding treatment before the catalytic hydrogenation using the above catalyst, thereby improving the activity of the catalyst. Specifically, the vulcanization treatment includes: loading the catalyst into the hydrogenation fixed bed reactor, and introducing vulcanized oil into the hydrogenation fixed bed reactor for vulcanization treatment, wherein the vulcanized oil is kerosene containing carbon disulfide, the hydrogen partial pressure of the vulcanization treatment is controlled to be 3-15MPa, the total space velocity is 0.1-2.0/h, and the volume ratio of hydrogen to the vulcanized oil is (200-): 1, the vulcanization time is 15-40h, and the vulcanization temperature is 250-400 ℃. After the sulfurization treatment is finished, the naphthenic base crude oil and/or the paraffin base crude oil can be introduced into the hydrogenation fixed bed reactor for catalytic hydrogenation reaction.
The implementation of the invention has at least the following advantages:
1. the low-temperature switching oil belongs to petroleum-based mineral low-temperature switching oil, and has the advantages of low pour point, good electrical property, good oxidation stability, environmental protection and the like;
2. when the low-temperature switch oil disclosed by the invention is filled into electrical equipment to operate, after short-circuit current occurs, the precipitation speed is high because free carbon in an oil sample is less, so that the insulation strength of the oil sample is ensured;
3. the low-temperature switch oil has small viscosity of an oil sample, so that the flowing speed of the oil becomes high, the heat dissipation performance of the switch equipment is improved, and when an oil circuit breaker is operated, the contact resistance is less, so that the arc extinguishing effect is enhanced, and the burning loss of the contact is reduced;
4. when the low-temperature switch oil has low flash point, the low-temperature switch oil has better gasification rate and evaporation rate, and is beneficial to extinguishing electric arcs generated between contacts of an oil circuit breaker;
5. compared with the processes of acid-base refining, dewaxing, synthetic oil adding and the like, the low-temperature switch oil produced by utilizing the high-pressure hydrogenation process and the precise fractionation process has the advantages of simple production process, low production cost, continuous large-scale production and the like.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The following examples are the preparation method of the low temperature switch oil of the present invention, wherein the raw material is naphthenic base crude oil and/or paraffin base crude oil, and the relevant parameters of the naphthenic base crude oil and the paraffin base crude oil are shown in the following table 1.
TABLE 1 cycloalkyl crude oil, Paraffin base crude oil related parameter Table
Item Naphthenic base oil Paraffin-based oils Test method
Kinematic viscosity at 40 ℃ in mm2/s 2200～3500 50～250 GB/T 265
Acid value of mgKOH/g 0.5～2.8 0.4～4.0 GB/T 4945
Pour point, DEG C ＞+5 ＞+5 GB/T 510
Example 1
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 4% of nickel oxide, 5% of molybdenum oxide, 3% of cobalt oxide, 3% of tungsten oxide and 85% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000051
Average pore volume of 0.2cm3Per g, average specific surface area of 190m3G, average strength of 100N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 4MPa, the vulcanization temperature is 380 ℃, and the total airspeed is 0.2h-1Hydrogen-oil volume ratio of 800:1, and vulcanization time of 15 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the present example, naphthenic base crude oil with a kinematic viscosity of 2500mm at 40 ℃ was selected as the raw material2The acid value was 1.0mgKOH/g and the pour point was 8 ℃.
The naphthenic base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 10MPa, the reaction temperature is 380 ℃, and the space velocity of the reaction volume is 0.5h-1Hydrogen-oil volume ratio 1000:1, formation after hydrogenationCrude oil.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, fractionating by reduced pressure distillation (with the operating pressure of 7.9KPa) to obtain 150-350 ℃ fraction, and transferring the fraction into a precision fractionation device (with the operating pressure of 0.9KPa) to cut 220-290 ℃ fraction, so as to obtain the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 60 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.38% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 2.
Example 2
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 10% of nickel oxide, 4% of molybdenum oxide, 2% of cobalt oxide, 7% of tungsten oxide and 77% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000062
Average pore volume of 1.5cm3(g) an average specific surface area of 250m3(ii) g, average strength 60N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 10MPa, the vulcanization temperature is 300 ℃, and the total airspeed is 1.5h-1Hydrogen-oil volume ratio of 700:1, and vulcanization time of 20 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the present example, naphthenic base crude oil with kinematic viscosity of 2200mm at 40 ℃ is selected as raw material2The acid value was 1.5mgKOH/g and the pour point was 6 ℃.
The naphthenic base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: inverse directionThe reaction pressure is 15MPa, the reaction temperature is 300 ℃, and the space velocity of the reaction volume is 1.5h-1Hydrogen-oil volume ratio 500:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, fractionating by reduced pressure distillation (with the operating pressure of 7.8KPa) to obtain 150-350 ℃ fraction, and transferring the fraction into a precision fractionation device (with the operating pressure of 0.8KPa) to cut 220-290 ℃ fraction, so as to obtain the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 65 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.30% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 2.
Example 3
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 15% of nickel oxide, 7% of molybdenum oxide, 2% of cobalt oxide, 4% of tungsten oxide and 74% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000061
Average pore volume of 1.8cm3(g) an average specific surface area of 300m3(ii) g, average strength 50N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 15MPa, the vulcanization temperature is 250 ℃, and the total space velocity is 0.5h-1Hydrogen-oil volume ratio of 600:1, and vulcanization time of 25 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the present example, naphthenic base crude oil with a kinematic viscosity of 3000mm at 40 ℃ is selected as the raw material2The acid value was 0.5mgKOH/g and the pour point was 8 ℃.
The naphthenic base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 18MPa, the reaction temperature is 200 ℃, and the space velocity of the reaction volume is 0.3h-1Hydrogen-oil volume ratio 1200: 1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, fractionating by reduced pressure distillation (the operating pressure is 8.0KPa) to obtain 150-350 ℃ fraction, and transferring the fraction into a precision fractionation device (the operating pressure is 0.8KPa) to cut 220-290 ℃ fraction, so as to obtain the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the base oil of the low-temperature switch to 60 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the proportion of 0.3 percent by mass fraction to obtain the mineral insulating oil of the low-temperature switch.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 2.
Example 4
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 12% of nickel oxide, 6% of molybdenum oxide, 4% of cobalt oxide, 4% of tungsten oxide and 74% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000071
Average pore volume of 0.2cm3Per g, average specific surface area of 100m3(ii) g, average strength 80N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 12MPa, the vulcanization temperature is 270 ℃, and the total space velocity is 2.0h-1Hydrogen-oil volume ratio of 500:1, and vulcanization time of 30 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In this example, naphthenic base crude oil was selected as the raw materialKinematic viscosity at 40 ℃ of 3500mm2The acid value was 2.0mgKOH/g and the pour point was 7 ℃.
The naphthenic base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 17MPa, the reaction temperature is 250 ℃, and the space velocity of the reaction volume is 1.0h-1Hydrogen-oil volume ratio 900:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, fractionating by reduced pressure distillation (with the operating pressure of 7.7KPa) to obtain 150-350 ℃ fraction, and transferring the fraction into a precision fractionation device (with the operating pressure of 0.9KPa) to cut 220-290 ℃ fraction, so as to obtain the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 65 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.35% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 3.
Example 5
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 18% of nickel oxide, 4% of molybdenum oxide, 3% of cobalt oxide, 6% of tungsten oxide and 69% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000081
Average pore volume of 0.1cm3Per g, average specific surface area of 350m3G, average strength of 20N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 13MPa, the vulcanization temperature is 260 ℃, and the total space velocity is 1.8h-1Hydrogen-oil volume ratio of 300:1, and vulcanization time of 40 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the present embodiment, naphthenic base crude oil with a kinematic viscosity of 2800mm at 40 ℃ is selected as a raw material2The acid value was 2.8mgKOH/g and the pour point was 8 ℃.
The naphthenic base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 12MPa, the reaction temperature is 350 ℃, and the space velocity of the reaction volume is 2.0h-1Hydrogen-oil volume ratio 400: 1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, fractionating by reduced pressure distillation (with the operating pressure of 7.9KPa) to obtain 150-350 ℃ fraction, and transferring the fraction into a precision fractionation device (with the operating pressure of 0.8KPa) to cut 220-290 ℃ fraction, so as to obtain the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the base oil of the low-temperature switch to 65 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.3% to obtain the mineral insulating oil of the low-temperature switch.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 3.
Example 6
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 17% of nickel oxide, 8% of molybdenum oxide, 2% of cobalt oxide, 8% of tungsten oxide and 65% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000091
Average pore volume of 1.7cm3Per g, average specific surface area 380m3G, average strength 70N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 10MPa, the vulcanization temperature is 300 ℃, and the total airspeed is 0.2h-1Hydrogen-oil volume ratio of 1000:1, and vulcanization time of 35 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the embodiment, naphthenic base crude oil is selected as a raw material, and the kinematic viscosity of the naphthenic base crude oil at 40 ℃ is 3200mm2The acid value was 2.5mgKOH/g and the pour point was 10 ℃.
The naphthenic base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 20MPa, the reaction temperature is 280 ℃, and the space velocity of the reaction volume is 0.4h-1Hydrogen-oil volume ratio 1000:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, fractionating by reduced pressure distillation (with the operating pressure of 7.9KPa) to obtain 150-350 ℃ fraction, and transferring the fraction into a precision fractionation device (with the operating pressure of 0.7KPa) to cut 220-290 ℃ fraction, so as to obtain the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the base oil of the low-temperature switch to 60 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.38% to obtain the mineral insulating oil of the low-temperature switch.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 3.
Example 7
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 16% of nickel oxide, 5% of molybdenum oxide, 2% of cobalt oxide, 8% of tungsten oxide and 69% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000101
Average pore volume of 1.9cm3(g) an average specific surface area of 370m3(ii) g, average strength 80N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 10MPa, the vulcanization temperature is 300 ℃, and the total airspeed is 1.8h-1Hydrogen-oil volume ratio of 900:1, and vulcanization time of 30 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In this example, paraffin-based crude oil was selected as the raw material, and the kinematic viscosity of the naphthenic base crude oil at 40 ℃ was 100mm2The acid value was 3.8mgKOH/g and the pour point was 7 ℃.
The paraffin base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 18MPa, the reaction temperature is 280 ℃, and the space velocity of the reaction volume is 0.4h-1Hydrogen-oil volume ratio 1000:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, carrying out reduced pressure distillation and fractionation (with the operating pressure of 7.9KPa) to obtain a fraction at 150-350 ℃, transferring the fraction into a precision fractionation device (with the operating pressure of 0.7KPa) to cut the fraction at 220-290 ℃, and obtaining the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 65 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.3% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 4.
Example 8
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 18% of nickel oxide, 3% of molybdenum oxide, 2% of cobalt oxide, 7% of tungsten oxide and 70% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000111
Average pore volume of 1.8cm3(g) an average specific surface area of 300m3G, average strength 70N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 12MPa, the vulcanization temperature is 350 ℃, and the total space velocity is 1.0h-1Hydrogen-oil volume ratio of 1000:1, and vulcanization time of 35 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the present example, paraffin-based crude oil was selected as the raw material, and the kinematic viscosity of the naphthenic base crude oil at 40 ℃ was 250mm2The acid value was 3.0mgKOH/g and the pour point was 7 ℃.
The paraffin base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 20MPa, the reaction temperature is 250 ℃, and the space velocity of the reaction volume is 0.7h-1Hydrogen-oil volume ratio 800:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, carrying out reduced pressure distillation and fractionation (with the operating pressure of 7.9KPa) to obtain a fraction at 150-350 ℃, transferring the fraction into a precision fractionation device (with the operating pressure of 0.8KPa) to cut the fraction at 220-290 ℃, and obtaining the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 55 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.25% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 4.
Example 9
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 10% of nickel oxide, 10% of molybdenum oxide, 2% of cobalt oxide, 4% of tungsten oxide and 74% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000112
Average pore volume of 1.8cm3(g) an average specific surface area of 250m3(ii) g, average strength 80N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 15MPa, the vulcanization temperature is 300 ℃, and the total airspeed is 2.0h-1Hydrogen-oil volume ratio of 500:1, and vulcanization time of 25 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In this example, a paraffin-based crude oil was selected as the raw material, and the kinematic viscosity of the naphthenic base crude oil at 40 ℃ was 80mm2The acid value was 1.0mgKOH/g and the pour point was 10 ℃.
The paraffin base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 18MPa, the reaction temperature is 200 ℃, and the space velocity of the reaction volume is 1.8h-1Hydrogen-oil volume ratio 500:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, fractionating by reduced pressure distillation (the operating pressure is 8.0KPa) to obtain 150-350 ℃ fraction, and transferring the fraction into a precision fractionation device (the operating pressure is 0.8KPa) to cut 220-290 ℃ fraction, so as to obtain the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 60 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.30% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 4.
Example 10
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 15% of nickel oxide, 8% of molybdenum oxide, 3% of cobalt oxide, 3% of tungsten oxide and 71% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000121
Average pore volume of 1.5cm3Per g, average specific surface area of 350m3(ii) a specific average strength of 90N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 9MPa, the vulcanization temperature is 250 ℃, and the total space velocity is 0.5h-1Hydrogen-oil volume ratio of 800:1, and vulcanization time of 15 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the present example, a paraffin-based crude oil was selected as a raw material, and the kinematic viscosity of the naphthenic base crude oil at 40 ℃ was 70mm2The acid value was 0.6mgKOH/g and the pour point was 8 ℃.
The paraffin base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 15MPa, the reaction temperature is 300 ℃, and the space velocity of the reaction volume is 1.0h-1Hydrogen-oil volume ratio 1200: 1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, carrying out reduced pressure distillation and fractionation (the operation pressure is 8.0KPa) to obtain a fraction at 150-350 ℃, transferring the fraction into a precision fractionation device (the operation pressure is 0.7KPa) to cut the fraction at 220-290 ℃, and obtaining the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 65 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.38% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 5.
Example 11
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: nickel oxide 17 percent of molybdenum oxide, 9 percent of cobalt oxide, 2 percent of tungsten oxide and 65 percent of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000131
Average pore volume of 0.4cm3(g) an average specific surface area of 200m3(ii) a mean strength of 65N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 8MPa, the vulcanization temperature is 280 ℃, and the total space velocity is 1.5h-1Hydrogen-oil volume ratio of 700:1, and vulcanization time of 35 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In this example, a paraffin-based crude oil was selected as the raw material, and the kinematic viscosity of the naphthenic base crude oil at 40 ℃ was 200mm2The acid value was 3.6mgKOH/g and the pour point was 6 ℃.
The paraffin base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 17MPa, the reaction temperature is 270 ℃, and the space velocity of the reaction volume is 0.9h-1Hydrogen-oil volume ratio 600:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, carrying out reduced pressure distillation and fractionation (the operation pressure is 8.1KPa) to obtain a fraction at 150-350 ℃, transferring the fraction into a precision fractionation device (the operation pressure is 0.7KPa) to cut the fraction at 220-290 ℃, and obtaining the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 65 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.3% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 5.
Example 12
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 10% of nickel oxide, 8% of molybdenum oxide, 3% of cobalt oxide, 6% of tungsten oxide and 73% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000141
Average pore volume of 1.8cm3Per g, average specific surface area 150m3G, average strength 70N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 6MPa, the vulcanization temperature is 370 ℃, and the total space velocity is 1.0h-1Hydrogen-oil volume ratio of 300:1, and vulcanization time of 17 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In this example, a paraffin-based crude oil was selected as the raw material, and the kinematic viscosity of the naphthenic base crude oil at 40 ℃ was 120mm2The acid value was 1.0mgKOH/g and the pour point was 6 ℃.
The paraffin base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 15MPa, the reaction temperature is 220 ℃, and the space velocity of the reaction volume is 1.0h-1Hydrogen-oil volume ratio 1000:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, carrying out reduced pressure distillation and fractionation (the operation pressure is 8.1KPa) to obtain a fraction at 150-350 ℃, transferring the fraction into a precision fractionation device (the operation pressure is 0.8KPa) to cut the fraction at 220-290 ℃, and obtaining the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 60 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.38% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 5.
Example 13
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 15% of nickel oxide, 7% of molybdenum oxide, 3% of cobalt oxide, 7% of tungsten oxide and 68% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000151
Average pore volume of 1.5cm3(g) an average specific surface area of 300m3G, average strength 70N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 12MPa, the vulcanization temperature is 300 ℃, and the total airspeed is 1.5h-1Hydrogen-oil volume ratio of 500:1, and vulcanization time of 30 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the embodiment, a mixture of naphthenic base crude oil and paraffin base crude oil is selected as the raw material, and the kinematic viscosity of the mixture crude oil at 40 ℃ is 1000mm2The acid value was 2.5mgKOH/g and the pour point was 6 ℃.
The mixture of the naphthenic base and the paraffin base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 10MPa, the reaction temperature is 300 ℃, and the space velocity of the reaction volume is 1.5h-1Hydrogen-oil volume ratio 800:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, carrying out reduced pressure distillation and fractionation (the operation pressure is 8.1KPa) to obtain a fraction at 150-350 ℃, transferring the fraction into a precision fractionation device (the operation pressure is 0.7KPa) to cut the fraction at 220-290 ℃, and obtaining the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 50 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.30% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 6.
Example 14
1. Catalyst presulfiding
The catalyst of the embodiment comprises the following components in percentage by weight: 10% of nickel oxide, 5% of molybdenum oxide, 3% of cobalt oxide, 5% of tungsten oxide and 77% of silicon oxide carrier. Wherein the catalyst has an average pore diameter of
Figure BDA0001385380970000161
Average pore volume of 1.0cm3(g) an average specific surface area of 250m3(ii) g, average strength 80N/mm.
The catalyst is filled into a hydrogenation reaction fixed bed reactor, and the sulfurized oil is CS containing carbon disulfide2The kerosene is vulcanized, and the vulcanizing process conditions are as follows: the partial pressure of hydrogen sulfide is 10MPa, the vulcanization temperature is 280 ℃, and the total space velocity is 1.7h-1Hydrogen-oil volume ratio of 800:1, and vulcanization time of 20 hours. The presulfurized catalyst is ready for use.
2. Catalytic hydrogenation
In the embodiment, a mixture of naphthenic base crude oil and paraffin base crude oil is selected as the raw material, and the kinematic viscosity of the mixture crude oil at 40 ℃ is 900mm2The acid value was 2.0mgKOH/g and the pour point was 7 ℃.
The mixture of the naphthenic base and the paraffin base crude oil passes through a hydrogenation process fixed bed reactor filled with a vulcanized catalyst, and the hydrogenation process conditions are as follows: the reaction pressure is 15MPa, the reaction temperature is 250 ℃, and the space velocity of the reaction volume is 1.0h-1Hydrogen-oil volume ratio 1000:1, crude oil is generated after hydrogenation is finished.
3. Double distillation
And (3) introducing the crude oil into a fractionation system, carrying out reduced pressure distillation and fractionation (the operation pressure is 8.1KPa) to obtain a fraction at 150-350 ℃, transferring the fraction into a precision fractionation device (the operation pressure is 0.8KPa) to cut the fraction at 220-290 ℃, and obtaining the low-temperature switch base oil.
4. Preparation of low-temperature switch oil
And heating the low-temperature switch base oil to 70 ℃, and adding 2, 6-di-tert-butyl-p-cresol according to the mass fraction of 0.30% to obtain the low-temperature switch mineral insulating oil.
The low-temperature switch mineral insulating oil of the embodiment meets various index requirements of the low-temperature switch oil in the standard GB2536-2011, and the specific parameters are shown in Table 6.
Table 2 analysis of key performance characteristics of the products of examples 1 to 3
Figure BDA0001385380970000162
Figure BDA0001385380970000171
Table 3 analysis of key performance characteristics of the products of examples 4 to 6
Figure BDA0001385380970000172
Table 4 analysis of key performance characteristics of the products of examples 7 to 9
Figure BDA0001385380970000173
Figure BDA0001385380970000181
Table 5 analysis of key performance characteristics of the products of examples 10 to 12
Figure BDA0001385380970000182
Table 6 analysis of key index properties of products of examples 13 and 14
Figure BDA0001385380970000183
As can be seen from tables 2 to 6: the low-temperature switching oil disclosed by the invention has higher cycloparaffin content and excellent solubility, can dissolve free carbon particles generated in the operation process of equipment, has a proper paraffin content, can promote the oil to be rapidly decomposed into gas under the action of high-temperature electric arc during the action of the switching equipment, is extremely favorable for arc extinction, and has a pour point which is 28-30 ℃ lower than that of the conventional low-temperature switching oil. Meanwhile, the PCA of the low-temperature switching oil is 0, so that the environmental protection performance of the low-temperature switching oil is proved.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.

Claims (3)

1. The low-temperature switch oil is characterized by comprising the following components: the low-temperature switch base oil comprises low-temperature switch base oil and a phenol antioxidant, wherein the weight of the phenol antioxidant accounts for 0.1-0.4% of that of the low-temperature switch base oil;
the low-temperature switch base oil is prepared by the following method:
1) introducing naphthenic base crude oil and/or paraffin base crude oil into a hydrogenation fixed bed reactor filled with a catalyst to generate crude oil;
wherein the volume ratio of the hydrogen to the naphthenic base crude oil and/or the paraffin base crude oil is (400- & 1200): 1, controlling the reaction temperature of the catalytic hydrogenation to be 200-400 ℃, the hydrogen partial pressure to be 10-20MPa, and the liquid volume space velocity to be 0.3-2.0/h;
the catalyst comprises the following components in percentage by weight: 3-18% of nickel oxide, 3-10% of molybdenum oxide, 1-4% of cobalt oxide, 3-8% of tungsten oxide and the balance of silicon oxide carrier;
the catalyst has an average pore diameter of
Figure FDA0003114783590000011
The average pore volume is 0.1-2.0cm3(g) average specific surface area of 100-3G, strength of 20-100N/mm;
the catalyst needs to be subjected to sulfurization treatment before use; the vulcanization treatment comprises the following steps: loading the catalyst into the hydrogenation fixed bed reactor, and introducing vulcanized oil into the hydrogenation fixed bed reactor for vulcanization treatment, wherein the vulcanized oil is kerosene containing carbon disulfide, the hydrogen partial pressure of the vulcanization treatment is controlled to be 3-15MPa, the total space velocity is 0.1-2.0/h, and the volume ratio of hydrogen to the vulcanized oil is (200-): 1, the vulcanization time is 15-40h, and the vulcanization temperature is 250-400 ℃;
2) subjecting the crude oil to a first distillation and collecting a fraction at 150-;
3) performing secondary distillation on the 150-350 ℃ fraction, and collecting a 220-290 ℃ fraction, wherein the 220-290 ℃ fraction is the low-temperature switch base oil;
according to the weight percentage, the aromatic hydrocarbon content of the low-temperature switch oil is 1% -3%, the naphthenic hydrocarbon content of the low-temperature switch oil is 60% -84%, the paraffin hydrocarbon content of the low-temperature switch oil is 15% -30%, and the pour point of the low-temperature switch oil is less than-70 ℃.
2. The method for preparing the low-temperature switching oil according to claim 1, comprising the steps of:
1) catalytically hydrogenating the naphthenic base crude oil and/or paraffin base crude oil to generate crude oil;
wherein the volume ratio of the hydrogen to the naphthenic base crude oil and/or the paraffin base crude oil is (400- & 1200): 1, controlling the reaction temperature of the catalytic hydrogenation to be 200-400 ℃, the hydrogen partial pressure to be 10-20MPa, and the liquid volume space velocity to be 0.3-2.0/h;
the catalyst comprises the following components in percentage by weight: 3-18% of nickel oxide, 3-10% of molybdenum oxide, 1-4% of cobalt oxide, 3-8% of tungsten oxide and the balance of silicon oxide carrier;
the catalyst has an average pore diameter of
Figure FDA0003114783590000021
The average pore volume is 0.1-2.0cm3(g) average specific surface area of 100-3G, strength of 20-100N/mm;
the catalyst needs to be subjected to sulfurization treatment before use; the vulcanization treatment comprises the following steps: loading the catalyst into the hydrogenation fixed bed reactor, and introducing vulcanized oil into the hydrogenation fixed bed reactor for vulcanization treatment, wherein the vulcanized oil is kerosene containing carbon disulfide, the hydrogen partial pressure of the vulcanization treatment is controlled to be 3-15MPa, the total space velocity is 0.1-2.0/h, and the volume ratio of hydrogen to the vulcanized oil is (200-): 1, the vulcanization time is 15-40h, and the vulcanization temperature is 250-400 ℃;
2) subjecting the crude oil to a first distillation and collecting a fraction at 150-;
3) performing second distillation on the fraction at the temperature of 150-350 ℃ in the step 2), and collecting a fraction at the temperature of 220-290 ℃, wherein the fraction at the temperature of 220-290 ℃ is the low-temperature switch base oil;
4) adding the phenol antioxidant into the low-temperature switch base oil to prepare the low-temperature switch oil; wherein the weight of the phenolic antioxidant accounts for 0.1-0.4% of the weight of the low-temperature switch base oil.
3. The method for preparing low-temperature switch oil according to claim 2, wherein the phenolic antioxidant is 2, 6-di-tert-butyl-p-cresol.
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