CN113969187A

CN113969187A - Method for producing refrigerating machine oil and transformer oil

Info

Publication number: CN113969187A
Application number: CN202010715336.1A
Authority: CN
Inventors: 李洪辉; 郭庆洲; 高杰; 王鲁强; 李洪宝
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2020-07-23
Filing date: 2020-07-23
Publication date: 2022-01-25
Anticipated expiration: 2040-07-23
Also published as: CN113969187B

Abstract

The application provides a method for producing refrigerating machine oil and transformer oil simultaneously, which comprises the following steps: (1) taking base oil with the viscosity index of less than 80 as a raw material, and reacting the base oil with the viscosity index of less than 80 in sequence by a first hydro-conversion reaction zone which is connected in series and is filled with a hydro-isomerization treatment catalyst and a second hydro-conversion reaction zone which is filled with a hydrofining catalyst to obtain hydro-conversion generated oil, wherein a carrier of the hydro-isomerization treatment catalyst comprises at least one selected from silicon oxide, aluminum oxide and silicon oxide-aluminum oxide and at least one shape-selective cracking molecular sieve; (2) and separating the oil generated by the hydro-conversion through distillation to obtain heavy fraction which is the refrigerating machine oil and light fraction which is the transformer oil. The invention can produce the refrigerating machine oil product and the transformer oil product with high added values in high yield by carrying out one-step hydro-conversion reaction on the low-value I type base oil product, thereby improving the economic benefit of enterprises.

Description

Method for producing refrigerating machine oil and transformer oil

Technical Field

The invention relates to the field of oil refining, in particular to a method for producing refrigerating machine oil and transformer oil.

Background

Because some refineries need to produce special wax products, the production must be carried out by adopting the traditional 'old three sets' process production flow, so that the refineries produce a large amount of API I base oil products while producing the special wax products. However, in recent years, due to the reduction of high-quality paraffin-based crude oil resources, the increase of the proportion of imported crude oil, frequent oil type change and poor quality, the quality of base oil products of I-class lubricating oil produced by the 'old three sets' process is reduced, the viscosity index of the base oil is low, and some products cannot meet the standard of the base oil of I-class, so that economic benefits cannot be brought to refineries.

In order to solve the problems of low value and difficult sale of low-end I base oil products for refineries, the characteristics of low paraffin content and high naphthene and aromatic hydrocarbon content in low-viscosity index (LVI) and medium-viscosity index (MVI) base oil are considered, and the low-pour-point low-paraffin-content medium-viscosity base oil just meets the requirements of low pour point, good compatibility with refrigerant, heat and oxidation stability and the like of refrigerating machine oil. The high-value-added refrigerator oil product can be converted into a high-value-added refrigerator oil product and a transformer oil product is a byproduct through a proper hydrogenation technology, and better economic benefits can be created for enterprises.

CN109852417A discloses a production method of naphthenic base special oil, which comprises the following steps: (1) mixing naphthenic base distillate oil and hydrogen, entering a hydrotreating reaction zone, and contacting with a hydrofining catalyst for reaction; (2) mixing the generated oil obtained in the step (1) with hydrogen, then feeding the mixture into a hydrogen mixing tank for hydrogen mixing, feeding the liquid phase effluent of the obtained saturated dissolved hydrogen into a complementary refining reaction zone, and contacting with a hydrogenation complementary refining catalyst for hydrogenation reaction; (3) and (3) carrying out gas-liquid separation on the supplementary refining reaction effluent obtained in the step (2), and fractionating the liquid to obtain corresponding special oil product fractions.

CN109852465A discloses a production process of naphthenic base lubricating oil, which comprises the following steps: (1) after being subjected to back flush filtration, the naphthenic base raw oil is mixed with hydrogen in a hydrogenation reactor, wherein the hydrogenation reactor consists of a first reactor, a second reactor and a third reactor; wherein, the first reactor is filled with a hydrogenation refining catalyst, and the raw oil undergoes hydrodemetallization, desulfurization, nitrogen reaction and aromatic saturation reaction; adding a hydrogenation pour point depression catalyst into the second reactor, and removing macromolecular normal paraffin with high pour point while further refining; a noble metal supplementary refining catalyst is additionally arranged in the third reactor, so that the low-temperature fluidity of the oil product is improved, and metal, sulfur and nitrogen impurities are removed; (2) the gas phase product obtained from the third reactor is subjected to hydrogen sulfide removal through an ammonia scrubber, then compressed through a recycle hydrogen compressor, and then returned to the hydrogenation reactor as recycle hydrogen; the obtained low-component gas is used as fuel to enter a fuel gas pipe network of the whole plant, and the acidic water is sent out of a boundary area for treatment; and the obtained low-fraction oil is sent to a fractionation system, byproducts fractionated by an atmospheric fractionating tower enter a naphtha oil tank area and a kerosene oil tank area respectively, and the main product is further fractionated by a reduced pressure fractionation tower to obtain transformer oil, refrigerator oil and a rubber plasticizer.

CN102311785B discloses a method for producing lube base oil by hydrogenating naphthenic distillate, which comprises the following steps: the naphthenic base distillate oil and hydrogen sequentially pass through a hydrotreating reaction zone, a hydrogenation pour point depression reaction zone and a hydrogenation refining reaction zone under the hydrogenation reaction condition, and the method is characterized in that: the hydrotreating reaction zone sequentially comprises a hydrotreating catalyst taking alumina as a carrier and a hydrotreating catalyst containing a modified beta molecular sieve according to the flowing direction of reaction materials; wherein the dosage of the hydrotreating catalyst containing the modified beta molecular sieve is 5 to 30 percent of the total volume of the two hydrotreating catalysts; the hydrofinishing catalyst takes gamma-Al 2O3 as a carrier, W and/or Mo of VIB group metals and Co and/or Ni of VIII group metals as active components, one or more elements of Si, P, F, B, Ti and Zr as auxiliaries, the VIB group elements account for 10 wt% -35 wt% of oxides, the VIII group elements account for 2.0 wt% -10.0 wt% of oxides, and the auxiliaries account for 0.1 wt% -10 wt% of the catalyst by elements.

The said process has long technological process and high production cost.

Disclosure of Invention

The invention aims to produce a refrigerating machine oil product and a transformer oil product with high yield from a low-value I-type base oil product.

The application provides a method for producing refrigerating machine oil and transformer oil simultaneously, which comprises the following steps:

(1) taking base oil with the viscosity index of less than 80 as a raw material, and reacting the base oil with the viscosity index of less than 80 in sequence by a first hydro-conversion reaction zone which is connected in series and is filled with a hydro-isomerization treatment catalyst and a second hydro-conversion reaction zone which is filled with a hydrofining catalyst to obtain hydro-conversion generated oil, wherein a carrier of the hydro-isomerization treatment catalyst comprises at least one selected from silicon oxide, aluminum oxide and silicon oxide-aluminum oxide and at least one shape-selective cracking molecular sieve;

(2) and separating the oil generated by the hydro-conversion through distillation to obtain heavy fraction which is the refrigerating machine oil and light fraction which is the transformer oil.

In one embodiment, the support for the hydroisomerization treatment catalyst is a silica-alumina and shape selective molecular sieve.

In one embodiment, the mass fraction of the silica-alumina is 60-90% and the mass fraction of the shape-selective cracking molecular sieve is 10-40% based on the total amount of the hydroisomerization catalyst carrier; preferably, the mass fraction of the silicon oxide-aluminum oxide is 70-85%, and the mass fraction of the shape-selective cracking molecular sieve is 15-30%.

In one embodiment, the hydroisomerization treatment catalyst comprises a hydrogenation-active metal component selected from one or more of nickel, cobalt, molybdenum, tungsten; the hydroisomerization treatment catalyst optionally contains a promoter component selected from one or more of fluorine, boron and phosphorus.

In one embodiment, the hydroisomerization catalyst comprises 5 to 20% by weight of nickel and/or cobalt in terms of oxide, 15 to 40% by weight of molybdenum and/or tungsten, and 0 to 9% by weight of one or more promoter components selected from fluorine, boron and phosphorus in terms of element, based on the total weight of the catalyst.

In one embodiment, the shape selective cracked molecular sieve is one or more of ZSM-5, ZSM-8, ZSM10, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-38, and ZSM-48.

In one embodiment, the hydrofining catalyst comprises a carrier and an active metal element and an optional auxiliary agent element which are loaded on the carrier, wherein the carrier is selected from one or more of alumina, silica-alumina and molecular sieve; the auxiliary agent element comprises one or more of fluorine, phosphorus and boron.

In one embodiment, the loading volume ratio of the hydroisomerization treatment catalyst and the hydrofinishing catalyst is from 0.1 to 10: 1.

In one embodiment, the first hydroconversion reaction zone and the second hydroconversion reaction zone are disposed in the same reactor; the first hydroconversion reaction zone is located before the second hydroconversion reaction zone, in terms of the feed flow direction.

In one embodiment, within the reactor, the hydrogenation reaction conditions are: the pressure is 5-20 MPa, the temperature is 250-400 ℃, the volume airspeed is 0.2-3 h < -1 >, and the volume ratio of hydrogen to oil is 100-1500.

In one embodiment, the base oil comprises a Low Viscosity Index (LVI) base oil having a viscosity index of less than 60 and/or a Medium Viscosity Index (MVI) base oil having a viscosity index of greater than or equal to 60 and less than 80.

In one embodiment, the distillation zone comprises one or more flash, atmospheric and vacuum distillation operating units.

According to the method provided by the invention, the LVI or MVI base oil is subjected to desulfurization, denitrification and partial aromatic saturation on the hydroisomerization treatment catalyst in the hydroconversion reaction zone, and normal paraffin in the raw material is isomerized to reduce the pour point of the raw material; then deep aromatic hydrocarbon saturation is carried out on a hydrofining catalyst, so that the final hydrogenated and converted oil meets the standard requirement of the refrigerator oil and the content requirement of the polycyclic aromatic hydrocarbon of the transformer oil. Finally, high-quality refrigerator oil and transformer oil products with different grades can be obtained through distillation separation. The invention can produce the refrigerating machine oil product and the transformer oil product with high added values in high yield by carrying out one-step hydro-conversion reaction on the low-value I type base oil product, thereby improving the economic benefit of enterprises.

Drawings

FIG. 1 is a schematic flow diagram of a method of the present invention.

Detailed Description

The technical solution of the present invention is further explained below according to specific embodiments. The scope of protection of the invention is not limited to the following examples, which are set forth for illustrative purposes only and are not intended to limit the invention in any way.

As shown in fig. 1, the present application provides a method for producing a refrigerator oil and concurrently producing a transformer oil, comprising:

In the present application, the first and second hydroconversion reaction zones may be located in two separate reactors connected in series, respectively, such that the hydroconversion reactions are carried out in the two reactors, respectively. In another embodiment, the first and second hydroconversion reaction zones may be located in the same reactor, such that the respective hydroconversion reactions are carried out sequentially in one reactor. Preferably, the first hydroconversion reaction zone is located before the second hydroconversion reaction zone according to the material flow direction, i.e. the raw oil is firstly hydroisomerized in the first hydroconversion reaction zoneAnd treating to obtain hydrogenated oil with low sulfur, low nitrogen, low pour point and partial aromatic saturation, and contacting with a hydrofining catalyst in a second hydrogenation conversion reaction zone to obtain hydrogenated oil with deep aromatic saturation. Therefore, sulfur and nitrogen in the raw material are removed, deep aromatic hydrocarbon saturation is realized, normal paraffin is isomerized to reduce the pour point of the raw material, and high-quality refrigerating machine oil and transformer oil products are produced with high yield. Such an embodiment is preferred. In this embodiment, the hydrogenation reaction conditions within the hydrogenation reactor are: the pressure is 5-20 MPa, the temperature is 250-400 ℃, and the volume airspeed is 0.2-3 h^-1The volume ratio of hydrogen to oil is 100-1500. In a specific embodiment, the reaction conditions are: the pressure is 5-20 MPa, the preferable pressure is 8-18 MPa, the temperature is 250-400 ℃, the preferable temperature is 280-380 ℃, and the volume space velocity is 0.2-3 h^-1Preferably 0.5 to 2 hours^-1The volume ratio of hydrogen to oil is 100 to 1500, preferably 200 to 1000.

In one embodiment, the base oil comprises a Low Viscosity Index (LVI) base oil having a viscosity index of less than 60 and/or a Medium Viscosity Index (MVI) base oil having a viscosity index of greater than or equal to 60 and less than 80. In one embodiment, the Low Viscosity Index (LVI) or Medium Viscosity Index (MVI) base oil is a group I base oil produced by a conventional solvent refining process.

Aiming at the problems of low value and difficult sale of LVI or MVI base oil products, the method provides a method for improving the added value of low-value base oil, and mainly removes sulfur and nitrogen in raw materials and deeply saturates aromatic hydrocarbons by using a novel hydroisomerization treatment catalyst and a hydrofining catalyst which are prepared by mixing and kneading silicon oxide-aluminum oxide and a shape-selective cracking molecular sieve as carriers in a hydroconversion reaction zone, isomerizes normal paraffins to reduce the pour point of the raw materials, and produces high-quality refrigerating machine oil and transformer oil products with high yield. The invention can produce the refrigerating machine oil product and the transformer oil product with high added values in high yield by carrying out the hydro-conversion reaction on the low-value I type base oil product, thereby improving the economic benefit of enterprises.

In the process of the present invention, the first hydrotreatment is carried out in the presence of a hydroisomerization catalyst. The application provides a hydroisomerization treatment catalyst, which comprises a carrier and a hydrogenation active metal component loaded on the carrier.

In one embodiment, the support of the hydroisomerization treatment catalyst comprises at least one member selected from the group consisting of silica, alumina, and silica-alumina, and at least one shape selective cracking molecular sieve. In one embodiment, the support of the hydroisomerization treatment catalyst comprises a silica-alumina and a shape selective molecular sieve. The carrier of the hydroisomerization catalyst is formed by mixing and kneading silica-alumina and a shape-selective cracking molecular sieve. On the basis of the total amount of the hydroisomerization catalyst carrier, the mass fraction of the silicon oxide-aluminum oxide is 60-90%, and the mass fraction of the shape-selective cracking molecular sieve is 10-40%. More preferably, the hydroisomerization catalyst comprises 70-85% by mass of silica-alumina and 15-30% by mass of a shape-selective cracking molecular sieve based on the total amount of the carrier.

In the hydroisomerization catalyst, the shape selective cracking molecular sieve is preferably at least one of ZSM-5, ZSM-8, ZSM10, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-38 and ZSM-48, and most preferably the shape selective cracking molecular sieve is ZSM-48.

In one embodiment, the hydrogenation-active metal component of the hydroisomerization treatment catalyst is one or more selected from the group consisting of nickel, cobalt, molybdenum, tungsten; nickel, molybdenum, tungsten are preferred. In one embodiment, the content of nickel and/or cobalt in terms of oxide is 5-20% based on the total amount of the hydroisomerization catalyst; the content of molybdenum and/or tungsten is 15-40%.

In one embodiment, the hydroisomerization treatment catalyst optionally contains a promoter component selected from one or more of fluorine, boron and phosphorus. In one embodiment, the content of the auxiliary component selected from one or more of fluorine, boron and phosphorus is 0 to 9% by element.

The preparation of the hydroisomerization catalyst may employ the following process: combining at least one selected from silica, alumina and silica-alumina and at least one shape-selective cracking molecular sieve in proportion to form a carrier; impregnating the carrier with a solution containing a compound of a hydrogenation active metal component and an optional compound of an auxiliary agent component, and roasting to obtain the hydroisomerization catalyst.

In one embodiment, during the preparation of the catalyst, it is also possible to optionally add organic additives in a molar ratio of 0 to 2: 1. in one embodiment, the organic additive is one or more selected from organic alcohol, organic acid and organic amine, and preferably the organic additive is organic acid.

In the process of the present invention, the second hydrotreatment is carried out in the presence of a hydrofinishing catalyst. In one embodiment, the hydrofining catalyst comprises a carrier and an active metal element and an optional auxiliary agent element which are loaded on the carrier, wherein the carrier is selected from one or more of alumina, silica-alumina and molecular sieve; the auxiliary agent element comprises one or more of fluorine, phosphorus and boron.

Specific examples of preferred hydrofinishing catalysts according to the present invention include the following hydrofinishing catalysts disclosed in the prior art: CN1105053A, CN1136069A, CN1169336A, CN1044378C and CN 1803283A. In particular, the hydrofinishing catalyst disclosed in CN1044378C has higher aromatic saturation performance when used in the present invention, and is therefore particularly suitable for use in the present invention.

In one embodiment, the loading volume ratio of the hydroisomerization treatment catalyst and the hydrofinishing catalyst is in the range of from 0.1 to 10:1, preferably from 0.5 to 5: 1.

after distillation, the refrigerating machine oil and the transformer oil with corresponding brands can be obtained. According to the viscosity, different grades of refrigerating machine oil can be obtained. The distillation range of the transformer oil is generally 280-350 ℃. In the present invention, the distillation process in the distillation zone is well known in the art and may generally include one or more of flash distillation, atmospheric distillation and vacuum distillation operating units as necessary to accomplish the desired separation.

The following examples further illustrate the invention.

The catalyst used in the examples of the present invention and the preparation method thereof are as follows:

1. hydroisomerization process catalyst 1

The hydroisomerization catalyst 1 used in embodiments 1 and 2 of the present invention uses a carrier obtained by mixing and kneading silica-alumina and a ZSM-48 molecular sieve, fluorine, phosphorus, and citric acid as auxiliary components, and nickel, molybdenum, and tungsten as active components. Wherein the mass fraction of the silicon oxide-aluminum oxide is 80% and the mass fraction of the shape-selective cracking molecular sieve is 20% based on the total amount of the carrier. Based on the total amount of the catalyst, the mass fraction of nickel is 8 percent and the mass fraction of molybdenum is 5 percent in terms of oxide. The mass fraction of tungsten is 28%, the mass fraction of phosphorus is 2.4%, the mass fraction of fluorine is 3.5% calculated by elements, and the balance is a carrier.

2. Hydroisomerization treatment catalyst 2

The hydroisomerization catalyst 2 used in embodiment 3 of the present invention is a carrier obtained by mixing and kneading silica-alumina and a ZSM-48 molecular sieve, fluorine and phosphorus are auxiliary components, citric acid is an organic additive, and nickel, molybdenum, and tungsten are active components. Wherein the mass fraction of the silicon oxide-aluminum oxide is 70 percent and the mass fraction of the shape-selective cracking molecular sieve is 30 percent based on the total amount of the carrier. Based on the total amount of the catalyst and calculated by oxides, the mass fraction of nickel is 8%, the mass fraction of molybdenum is 5%, and the mass fraction of tungsten is 28%; calculated by elements, the mass fraction of phosphorus is 2.4%, the mass fraction of fluorine is 3.5%, and the balance is the carrier.

3. Hydroisomerization treatment catalyst 3

The hydroisomerization catalyst 3 used in embodiment 4 of the present invention is a carrier obtained by mixing and kneading silica-alumina and a ZSM-48 molecular sieve, fluorine and phosphorus are auxiliary components, citric acid is an organic additive, and nickel, molybdenum, and tungsten are active components. Wherein the mass fraction of the silicon oxide-aluminum oxide is 80% and the mass fraction of the shape-selective cracking molecular sieve is 20% based on the total amount of the carrier. Based on the total amount of the catalyst and calculated by oxides, the mass fraction of nickel is 5%, the mass fraction of molybdenum is 2.1%, and the mass fraction of tungsten is 21%; calculated by elements, the mass fraction of phosphorus is 0.8%, the mass fraction of fluorine is 2.5%, and the balance is the carrier.

The preparation method comprises the following steps:

(1) mixing a silicon oxide-aluminum oxide carrier and a ZSM-48 shape-selective cracking molecular sieve according to a proportion, extruding and forming, drying at 120 ℃ for 5 hours, and roasting at 500 ℃ for 3 hours to obtain a catalyst carrier;

(2) preparing mixed solution of phosphoric acid, ammonium fluoride, citric acid, nickel nitrate, ammonium molybdate and ammonium metatungstate according to a proportion, impregnating a catalyst carrier for 2 hours, drying at 120 ℃ for 2 hours, and finally roasting at 500 ℃ for 4 hours to obtain the hydroisomerization catalyst.

4. Hydrorefining catalyst

The hydrorefining catalyst used in the examples of the present invention was prepared according to example 1 in CN1044378C, and the catalyst composition was 2.7 mass% of nickel oxide, 27.7 mass% of tungsten oxide, 4.9 mass% of fluorine, and the balance of a carrier.

Example 1

This example starts from an MVI 150 base oil, the properties of which are shown in Table 1.

The feedstock was processed according to the process flow of figure 1. Wherein the hydrogenation conversion reaction zone is respectively filled with a hydroisomerization catalyst 1 and a hydrofining catalyst, the hydroisomerization catalyst 1 is positioned at the upper part, the hydrofining catalyst is positioned at the lower part, the filling volume ratio is 1:1, and the operation conditions are shown in Table 2. The properties of the refrigerator oil obtained by the hydroconversion reaction zone and subjected to the separation of the hydroconversion-derived oil in the distillation zone are shown in Table 3, and the properties of the transformer oil are shown in Table 4.

TABLE 1

TABLE 2

Process conditions	Hydroconversion reaction zone
		Partial pressure of hydrogen/MPa	16.0
Reaction temperature/. degree.C	330
		Volume space velocity/h-1	1.0
Hydrogen to oil ratio/(v/v)	500

TABLE 3

Product Properties	No. 32 refrigerator oil
		Yield/%	69.3
Viscosity at 40 ℃/(mm)²/s)	28.96
		Sulfur content/. mu.g.g^-1	<10
Nitrogen content/microgram g^-1	<1
		Pour point/. degree.C	-33
Saybolt color comparison/number	>+30
		Flash point/. degree.C	169
Total acid value/(mgKOH/g)	<0.01

TABLE 4

Example 2

This example starts from an MVI 350 base oil, the properties of which are shown in Table 5.

The feedstock was processed according to the process flow of figure 1. Wherein the hydrogenation conversion reaction zone is filled with a hydroisomerization catalyst 1 and a hydrofining catalyst, the hydroisomerization catalyst 1 is positioned at the upper part, the hydrofining catalyst is positioned at the lower part, the filling volume ratio is 2:3, the operation conditions are shown in table 6, the properties of the refrigerator oil obtained by the hydrogenation conversion reaction zone after being separated by the distillation zone are shown in table 7, and the properties of the transformer oil are shown in table 8.

TABLE 5

TABLE 6

Process conditions	Hydroconversion reaction zone
		Partial pressure of hydrogen/MPa	16.0
Reaction temperature/. degree.C	360
		Volume space velocity/h^-1	0.8
Hydrogen to oil ratio/(v/v)	500

TABLE 7

Product Properties	Number 68 refrigerator oil
		Yield/%	66.7
Viscosity at 40 ℃/(mm)²/s)	62.49
		Sulfur content/. mu.g.g^-1	<10
Nitrogen content/microgram g^-1	<1
		Pour point/. degree.C	-27
Saybolt color comparison/number	>+30
		Flash point/. degree.C	186
Total acid value/(mgKOH/g)	<0.01

TABLE 8

Example 3

The example used the same starting material as in example 2, which was processed according to the process scheme of FIG. 1. Wherein the hydrogenation conversion reaction zone is filled with a hydroisomerization catalyst 2 and a hydrofining catalyst, the hydroisomerization catalyst 2 is positioned at the upper part, the hydrofining catalyst is positioned at the lower part, the filling volume ratio is 2:3, the operation conditions are shown in table 9, the properties of the refrigerator oil obtained by the hydrogenation conversion reaction zone after being separated by the distillation zone are shown in table 10, and the properties of the transformer oil are shown in table 11.

TABLE 9

Process conditions	Hydroconversion reaction zone
		Partial pressure of hydrogen/MPa	16.0
Reaction temperature/. degree.C	350
		Volume space velocity/h^-1	0.8
Hydrogen to oil ratio/(v/v)	500

Watch 10

Product Properties	Number 68 refrigerator oil
		Yield/%	63.4
Viscosity at 40 ℃/(mm)²/s)	61.86
		Sulfur content/. mu.g.g^-1	<10
Nitrogen content/microgram g^-1	<1
		Pour point/. degree.C	-27
Saybolt color comparison/number	>+30
		Flash point/. degree.C	181
Total acid value/(mgKOH/g)	<0.01

TABLE 11

Product Properties	LCSET-30 ℃ transformer oil
		Yield/%	22.8
Viscosity at 40 ℃/(mm)²/s)	11.38
		Sulfur content/. mu.g.g^-1	<10
Nitrogen content/microgram g^-1	<1
		Pour point/. degree.C	-42
Flash point/. degree.C	142
		Total acid value/(mgKOH/g)	<0.01
Content of condensed ring aromatic hydrocarbons/%)	<3

Example 4

The example used the same starting material as in example 2, which was processed according to the process scheme of FIG. 1. Wherein the hydrogenation conversion reaction zone is filled with a hydroisomerization treatment catalyst 3 and a hydrofining catalyst, the hydroisomerization treatment catalyst 3 is positioned at the upper part, the hydrofining catalyst is positioned at the lower part, the filling volume ratio is 2:3, the operation conditions are shown in table 12, the properties of the refrigerator oil obtained by the hydrogenation conversion reaction zone after being separated by the distillation zone are shown in table 13, and the properties of the transformer oil are shown in table 14.

TABLE 12

Process conditions	Hydroconversion reaction zone
		Partial pressure of hydrogen/MPa	16.0
Reaction temperature/. degree.C	350
		Volume space velocity/h^-1	0.6
Hydrogen to oil ratio/(v/v)	500

Watch 13

TABLE 14

Product Properties	LCSET-30 ℃ transformer oil
		Yield/%	23.7
Viscosity at 40 ℃/(mm)²/s)	11.49
		Sulfur content/. mu.g.g^-1	<10
Nitrogen content/microgram g^-1	<1
		Pour point/. degree.C	-42
Flash point/. degree.C	140
		Total acid value/(mgKOH/g)	<0.01
Content of condensed ring aromatic hydrocarbons/%)	<3

Comparative example 1

This comparative example uses the same starting material as in example 1 and processes the starting material according to the process scheme of figure 1. Wherein a hydroprocessing catalyst RIPP industrial agent RL-2 without a shape selective cracking molecular sieve and a hydrofining catalyst are filled in the hydroconversion reaction zone, the hydroprocessing catalyst is positioned at the upper part, the hydrofining catalyst is positioned at the lower part, the filling volume ratio is 1:1, the operation conditions are shown in table 15, the properties of the refrigerator oil obtained by the hydroconversion reaction zone after the oil is separated by a distillation zone are shown in table 16, and the properties of the transformer oil are shown in table 17.

Watch 15

TABLE 16

Product Properties	No. 32 refrigerator oil
		Yield/%	59.8
Viscosity at 40 ℃/(mm)²/s)	28.16
		Sulfur content/. mu.g.g^-1	<10
Nitrogen content/microgram g^-1	<1
		Pour point/. degree.C	-33
Saybolt color comparison/number	>+30
		Flash point/. degree.C	163
Total acid value/(mgKOH/g)	<0.01

TABLE 17

Product Properties	LCSET-30 ℃ transformer oil
		Yield/%	18.5
Viscosity at 40 ℃/(mm)²/s)	10.62
		Sulfur content/. mu.g.g^-1	<10
Nitrogen content/microgram g^-1	<1
		Pour point/. degree.C	-42
Flash point/. degree.C	138
		Total acid value/(mgKOH/g)	<0.01
Content of condensed ring aromatic hydrocarbons/%)	<3

Comparative example 2

This comparative example uses the same starting material as in example 2 and processes the starting material according to the process scheme of figure 1. The hydrogenation conversion reaction zone is filled with a hydrogenation treatment catalyst RIPP industrial agent RL-2 without a shape selective cracking molecular sieve, the hydrogenation treatment catalyst is positioned at the upper part, the hydrofining catalyst is positioned at the lower part, the filling volume ratio is 2:3, the operation conditions are shown in a table 18, the properties of the refrigerating machine oil obtained by the hydrogenation conversion reaction zone after being separated by a distillation zone are shown in a table 19, and the properties of the transformer oil are shown in a table 20.

Watch 18

Process conditions	Hydroconversion reaction zone
		Partial pressure of hydrogen/MPa	16.0
Reaction temperature/. degree.C	375
		Volume space velocity/h^-1	0.6
Hydrogen to oil ratio/(v/v)	500

Watch 19

Product Properties	Number 68 refrigerator oil
		Yield/%	57.2
Viscosity at 40 ℃/(mm)²/s)	61.38
		Sulfur content/. mu.g.g^-1	<10
Nitrogen content/microgram g^-1	<1
		Pour point/. degree.C	-27
Saybolt color comparison/number	>+30
		Flash point/. degree.C	178
Total acid value/(mgKOH/g)	<0.01

Watch 20

Comparing example 1 and comparative example 1, it can be found that the method of the present application can obtain refrigerator oil and transformer oil of corresponding grades with higher yield, and meanwhile, the obtained refrigerator oil has higher viscosity, higher flash point and better thermal stability. Similar results were obtained comparing example 2 and comparative example 2. The result shows that the method can convert the I-type base oil products such as Low Viscosity Index (LVI) and Medium Viscosity Index (MVI) base oil with low product value into the refrigerator oil and transformer oil products with high added values in high yield, and improve the economic benefit of enterprises.

It should be noted by those skilled in the art that the described embodiments of the present invention are merely exemplary and that various other substitutions, alterations, and modifications may be made within the scope of the present invention. Accordingly, the present invention is not limited to the above-described embodiments, but is only limited by the claims.

Claims

1. A method for producing refrigerating machine oil and transformer oil at the same time comprises the following steps:

2. The process of claim 1 wherein the support of the hydroisomerization treatment catalyst is a silica-alumina and a shape selective molecular sieve.

3. The method of claim 2, wherein the mass fraction of the silica-alumina is 60-90% and the mass fraction of the shape selective cracking molecular sieve is 10-40% based on the total amount of the hydroisomerization treatment catalyst support; preferably, the mass fraction of the silicon oxide-aluminum oxide is 70-85%, and the mass fraction of the shape-selective cracking molecular sieve is 15-30%.

4. The process of claim 1 wherein the hydroisomerization treatment catalyst comprises a hydrogenation-active metal component selected from one or more of nickel, cobalt, molybdenum, tungsten; the hydroisomerization treatment catalyst optionally contains a promoter component selected from one or more of fluorine, boron and phosphorus.

5. The process of claim 4, wherein the hydroisomerization catalyst comprises 5 to 20% by weight, calculated as oxide, of nickel and/or cobalt, 15 to 40% by weight, molybdenum and/or tungsten, and 0 to 9% by weight, calculated as element, of one or more promoter components selected from fluorine, boron and phosphorus; the molar ratio of the organic additive to the sum of the hydrogenation active metal components calculated by oxides is 0-2: 1.

6. the process of any one of claims 1-5, wherein the shape selective cracking molecular sieve is one or more of ZSM-5, ZSM-8, ZSM10, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-38, and ZSM-48.

7. The method of claim 1, wherein the hydrofining catalyst comprises a carrier and an active metal element and an optional auxiliary element which are loaded on the carrier, wherein the carrier is selected from one or more of alumina, silica-alumina and molecular sieve; the auxiliary agent element comprises one or more of fluorine, phosphorus and boron.

8. The process of claim 1, wherein the loading volume ratio of the hydroisomerization treatment catalyst and the hydrofinishing catalyst is from 0.1 to 10: 1.

9. The process of claim 1, wherein the first and second hydroconversion reaction zones are disposed in the same reactor; the first hydroconversion reaction zone is located before the second hydroconversion reaction zone, in terms of the feed flow direction.

10. The process of claim 9, wherein, within the reactor, the hydrogenation reaction conditions are: the pressure is 5-20 MPa, the temperature is 250-400 ℃, and the volume airspeed is 0.2-3 h^-1The volume ratio of hydrogen to oil is 100-1500.

11. The method of claim 1, wherein the base oil comprises a Low Viscosity Index (LVI) base oil having a viscosity index of less than 60 and/or a Medium Viscosity Index (MVI) base oil having a viscosity index of greater than or equal to 60 and less than 80.