JP2014062271A - Lubricant base oil and production method of the same, and lubricant composition - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a lubricant base oil that can satisfy a viscosity-temperature characteristic and a low temperature viscosity characteristic by a high level and with good balance, and a production method of the same; and a lubricant composition that includes the lubricant base oil.SOLUTION: A lubricant base oil is that a urea adduct value is at most 7 mass%, a viscosity index is at least 100, and a content of a saturation component is at least 90 mass% based on the total amount of a lubricant base oil. Moreover, a production method of a lubricant base oil includes a process in which hydrocracking is performed for raw oil including normal paraffin so that a urea adduct value of a processed product may be at most 7 mass%, a viscosity index may be at least 100, and a content of a saturation component may be at least 90 mass% based on the total amount of a lubricant base oil. Moreover, a lubricant composition includes the lubricant base oil.

Description

  The present invention relates to a lubricating base oil, a method for producing the same, and a lubricating oil composition.

  Conventionally, in the lubricating oil field, various additives such as highly refined mineral oil and other base oils are blended to improve the characteristics of the lubricating oil such as viscosity-temperature characteristics and thermal / oxidative stability. (For example, refer to Patent Documents 1 to 4).

JP-A-4-36391 Japanese Patent Laid-Open No. 4-68082 Japanese Patent Laid-Open No. 4-120193 Japanese Patent Laid-Open No. 2007-246659

  However, recently, the required characteristics of the lubricating oil have become higher and the lubricating base oil as described in Patent Documents 1 to 4 is not necessarily sufficient in terms of viscosity-temperature characteristics and low-temperature viscosity characteristics. I can not say. In addition, when these conventional lubricating base oils are used, there is a limit to the improvement of the above characteristics by the addition of additives.

  For example, due to increasing interest in energy conservation in recent years, or reduction in carbon dioxide emissions due to COP3, the friction performance of lubricating oils used is improved in factories that handle many machines and in the automobile industry that directly emits carbon dioxide. However, there is a movement to promote energy saving. In order to improve the friction characteristics of lubricating oil, there are a method of improving with an additive such as an oily agent and a method of improving the viscosity characteristics by improving the viscosity-temperature characteristics of the base oil to reduce the frictional resistance. . In particular, various studies have been made on additives, and friction reduction is being promoted. On the other hand, as an improvement from the lubricating base oil side, development of a so-called high viscosity index base oil that reduces the change in viscosity due to temperature is underway, and in particular, GTL using FT (Fischer-Tropsch) synthetic wax as a raw material. (Gas Liquid) Base oil is being developed. Furthermore, in the field of automobiles, in order to reduce the viscous resistance at the time of starting at a low temperature, studies have been made to reduce the viscosity at a low temperature.

  However, it is very difficult to impart sufficient characteristics to the lubricating base oil for energy saving. For this reason, it is currently dependent on additives such as pour point depressants, but pour point depressants do not have a constant effect, are less effective depending on the base oil production method, and obtain stable low temperature characteristics. It is difficult.

  The present invention has been made in view of such circumstances, and its purpose is excellent in viscosity-temperature characteristics and low-temperature viscosity characteristics, and when an additive is blended, the function of the additive is enhanced. An object of the present invention is to provide a lubricating base oil that can be expressed at a standard, a method for producing the same, and a lubricating oil composition using the lubricating base oil.

In order to solve the above problems, the present invention is obtained from a raw material oil containing normal paraffin, has a urea adduct value of 7% by mass or less, a viscosity index of 100 or more, and a saturated content. The lubricating base oil is characterized by being 90% by mass or more based on the total amount of the lubricating base oil.
The present invention also provides a lubricating base oil obtained from a raw material oil containing normal paraffin, having a urea adduct value of 7% by mass or less and a viscosity index of 100 or more.

  The urea adduct value as used in the present invention is measured by the following method. 100 g of weighed sample oil (lubricating base oil) is placed in a round bottom flask, 200 g of urea, 360 ml of toluene and 40 ml of methanol are added and stirred at room temperature for 6 hours. As a result, white granular crystals are produced as urea adducts in the reaction solution. The reaction solution is filtered through a 1 micron filter to collect the produced white granular crystals, and the obtained crystals are washed 6 times with 50 ml of toluene. The recovered white crystals are put in a flask, 300 ml of pure water and 300 ml of toluene are added, and the mixture is stirred at 80 ° C. for 1 hour. The aqueous phase is separated and removed with a separatory funnel, and the toluene phase is washed three times with 300 ml of pure water. A desiccant (sodium sulfate) is added to the toluene phase for dehydration, and then toluene is distilled off. The ratio (mass percentage) of the urea adduct thus obtained to the sample oil is defined as the urea adduct value.

  Moreover, the viscosity index as used in the present invention, and the kinematic viscosity at 40 ° C. and the kinematic viscosity at 100 ° C. described later are the kinematic viscosity and viscosity index at 40 ° C. or 100 ° C. measured according to JIS K 2283-1993, respectively. Means.

  According to the lubricating base oil of the present invention, when the urea adduct value and the viscosity index satisfy the above-mentioned conditions, the viscosity-temperature characteristic and the low-temperature viscosity characteristic can be satisfied at a high level. In addition, when an additive such as a pour point depressant is blended in the lubricating base oil of the present invention, the effect of the addition can be effectively expressed. Therefore, the lubricating base oil of the present invention is very useful as a lubricating base oil that meets the recent demand for compatibility between viscosity-temperature characteristics and low-temperature viscosity characteristics. Furthermore, according to the lubricating base oil of the present invention, viscosity resistance and stirring resistance in the practical temperature range can be reduced by the excellent viscosity-temperature characteristics described above. In particular, the lubricating base oil of the present invention can exert its effect by greatly reducing viscosity resistance and stirring resistance under low temperature conditions of 0 ° C. or lower, and an apparatus to which the lubricating base oil is applied. It is very useful in that it can reduce energy loss and achieve energy saving.

  Conventionally, improvement of the isomerization rate from normal paraffin to isoparaffin has been studied in the method of refining lubricating base oil by hydrocracking, but according to the study by the present inventors, the remaining amount of normal paraffin is merely It is difficult to sufficiently improve the low-temperature viscosity characteristics only by reducing the viscosity. That is, the isoparaffin produced by hydrocracking also contains components that adversely affect the low-temperature viscosity characteristics, but this point is not fully recognized in conventional evaluation methods. Analytical techniques such as gas chromatography (GC) and NMR are applied to the analysis of normal paraffin and isoparaffin. In these analytical techniques, components that adversely affect the low-temperature viscosity characteristics are separated or specified from isoparaffin. This cannot be said to be practically effective because it requires complicated work and a lot of time.

  On the other hand, in the measurement of the urea adduct value in the present invention, as urea adduct, a component that adversely affects low-temperature viscosity characteristics among isoparaffins, and further when normal paraffin remains in the lubricating base oil Since the normal paraffin can be collected accurately and reliably, it is excellent as an evaluation index of the low temperature viscosity characteristics of the lubricating base oil. The inventors of the present invention have analyzed by using GC and NMR that the main component of the urea adduct is a normal paraffin and an isoparaffin urea adduct having 6 or more carbon atoms from the end of the main chain to the branch position. Confirm that there is.

In addition, the present invention provides a carrier having a fraction of NH ₃ desorption amount at 300 to 800 ° C. with respect to the total desorption amount of NH _{3 in} the evaluation of NH ₃ desorption temperature dependency of 80% or less in the periodic table group VIa A first step of preparing a hydrocracking catalyst on which at least one kind of metal and at least one kind of group VIII metal are supported; and 50% by volume or more of slack wax in the presence of the hydrocracking catalyst A second step of hydrocracking the raw material oil containing at a hydrogen partial pressure of 0.1 to 14 MPa, an average reaction temperature of 230 to 430 ° C., LHSV of 0.3 to 3.0 hr ⁻¹ , and a hydrogen oil ratio of 50 to 14000 scf / b; A third step in which the cracked product oil obtained in the second step is separated by distillation to obtain a lubricating oil fraction, and the lubricating oil fraction obtained in the third step is dewaxed to give a urea adduct value of 7 Less than mass%, viscosity A fourth step of obtaining a lubricating base oil having a number of 100 or more and a saturated content of 90% by mass or more based on the total amount of the lubricating base oil. A method for producing an oil base oil is provided. The present invention is also recovered by distillation separation from the fifth step of hydrocracking a feedstock containing paraffinic hydrocarbons in the presence of a catalyst, and the product obtained in the fifth step or the product. The lubricating oil fraction is dewaxed, the urea adduct value is 7% by mass or less, the viscosity index is 100 or more, and the saturated content is 90% by mass based on the total amount of the lubricating base oil. And a sixth step of obtaining the lubricating base oil as described above.
In addition, the present invention provides a carrier having a fraction of NH ₃ desorption amount at 300 to 800 ° C. with respect to the total desorption amount of NH _{3 in} the evaluation of NH ₃ desorption temperature dependency of 80% or less in the periodic table group VIa A first step of preparing a hydrocracking catalyst on which at least one kind of metal and at least one kind of group VIII metal are supported; and 50% by volume or more of slack wax in the presence of the hydrocracking catalyst A second step of hydrocracking the raw material oil containing at a hydrogen partial pressure of 0.1 to 14 MPa, an average reaction temperature of 230 to 430 ° C., LHSV of 0.3 to 3.0 hr ⁻¹ , and a hydrogen oil ratio of 50 to 14000 scf / b; A third step in which the cracked product oil obtained in the second step is separated by distillation to obtain a lubricating oil fraction, and the lubricating oil fraction obtained in the third step is dewaxed to give a urea adduct value of 7 Less than mass% and viscosity Index provides a method for producing a lubricant base oil, characterized in that it comprises a fourth step of obtaining a lubricating base oil is 100 or more, a. The present invention is also recovered by distillation separation from the fifth step of hydrocracking a feedstock containing paraffinic hydrocarbons in the presence of a catalyst, and the product obtained in the fifth step or the product. A sixth step of dewaxing the lubricating oil fraction to obtain a lubricating base oil having a urea adduct value of 7% by mass or less and a viscosity index of 100 or more. A manufacturing method is provided.

  According to the method for producing a lubricating base oil of the present invention, hydrocracking is carried out on a feedstock containing normal paraffin so that the urea adduct value of the product to be treated is 7% by mass or less and the viscosity index is 100 or more. By performing the above, it is possible to reliably obtain a lubricating base oil having both a viscosity-temperature characteristic and a low-temperature viscosity characteristic at a high level.

  The present invention also provides a lubricating oil composition comprising the lubricating base oil of the present invention.

  Since the lubricating oil composition of the present invention contains the lubricating base oil of the present invention having the above-mentioned excellent characteristics, it has excellent viscosity-temperature characteristics and low-temperature viscosity characteristics, and when it contains an additive, The function of the agent can be expressed at a higher level.

  As described above, according to the present invention, a lubricating oil base that is excellent in viscosity-temperature characteristics and low-temperature viscosity characteristics and can exhibit the function of the additive at a higher level when the additive is blended. Provided are an oil and a method for producing the same, and a lubricating oil composition using the lubricating base oil.

  Hereinafter, preferred embodiments of the present invention will be described in detail.

  The lubricating base oil of the present invention has a urea adduct value of 7% by mass or less and a viscosity index of 100 or more.

  The urea adduct value of the lubricating base oil of the present invention needs to be 7% by mass or less as described above from the viewpoint of improving the low temperature viscosity characteristics without impairing the viscosity-temperature characteristics and from the viewpoint of friction characteristics at low temperatures. Preferably, it is 6.9 mass% or less, More preferably, it is 6.8 mass% or less, More preferably, it is 6.75 mass% or less. In addition, the urea adduct value of the lubricating base oil may be 0% by mass, but a lubricating base oil having sufficient low-temperature viscosity characteristics and a high viscosity index can be obtained, and the isomerization conditions can be relaxed, making it economical. From the viewpoint of excellent properties, it is preferably 0.1% by mass or more, more preferably 0.5% by mass or more, and particularly preferably 0.8% by mass or more.

  The viscosity index of the lubricating base oil of the present invention needs to be 100 or more as described above from the viewpoint of viscosity-temperature characteristics, preferably 110 or more, more preferably 120 or more, still more preferably 130 or more, Especially preferably, it is 140 or more. When the viscosity index is less than 100, there is a possibility that effective fuel saving characteristics cannot be obtained.

  The lubricating base oil of the present invention is not particularly limited as long as it satisfies the condition that the urea adduct value is 7% by mass or less and the viscosity index is 100 or more. Specifically, a lubricating oil fraction obtained by atmospheric distillation and / or vacuum distillation of crude oil is subjected to solvent removal, solvent extraction, hydrocracking, solvent dewaxing, catalytic dewaxing, hydrorefining, sulfuric acid Of paraffinic mineral oil, or normal paraffinic base oil, isoparaffinic base oil, etc. purified by combining one or more of the purification treatments such as washing and clay treatment, the urea adduct value is 7 mass % Or less and a viscosity index of 100 or more is satisfied. These lubricating base oils may be used alone or in combination of two or more.

As a preferable example of the lubricating base oil of the present invention, the following base oils (1) to (8) are used as raw materials, and this raw oil and / or a lubricating oil fraction recovered from this raw oil is used in a predetermined manner. The base oil obtained by refine | purifying with a refinement | purification method and collect | recovering lubricating oil fractions can be mentioned.
(1) Distilled oil by atmospheric distillation of paraffinic crude oil and / or mixed base crude oil (2) Distilled oil by vacuum distillation of atmospheric distillation residue of paraffinic crude oil and / or mixed base crude oil ( WVGO)
(3) Wax (such as slack wax) obtained by the lubricant dewaxing process and / or synthetic wax (Fischer-Tropsch wax, GTL wax, etc.) obtained by the gas-liquid (GTL) process, etc.
(4) One or two or more mixed oils selected from base oils (1) to (3) and / or mild hydrocracking treatment oils of the mixed oils (5) selected from base oils (1) to (4) 2 or more kinds of mixed oils (6) Base oil (1), (2), (3), (4) or (5) debris oil (DAO)
(7) Mild hydrocracking treatment oil (MHC) of base oil (6)
(8) Two or more mixed oils selected from base oils (1) to (7).

  The above-mentioned predetermined purification methods include hydrorefining such as hydrocracking and hydrofinishing; solvent refining such as furfural solvent extraction; dewaxing such as solvent dewaxing; white clay refining using acid clay or activated clay; sulfuric acid A chemical (acid or alkali) cleaning such as cleaning and caustic soda cleaning is preferable. In the present invention, one of these purification methods may be performed alone, or two or more may be combined. Moreover, when combining 2 or more types of purification methods, the order in particular is not restrict | limited, It can select suitably.

Furthermore, as the lubricating base oil of the present invention, a base oil selected from the above base oils (1) to (8) or a lubricating oil fraction recovered from the base oil is obtained by performing a predetermined treatment. Base oil (9) or (10) is particularly preferred.
(9) The base oil selected from the base oils (1) to (8) or the lubricating oil fraction recovered from the base oil is hydrocracked and recovered from the product or the product by distillation or the like. A hydrocracked mineral oil obtained by performing a dewaxing treatment such as solvent dewaxing on the lubricating oil fraction or by distillation after the dewaxing treatment is selected from the above base oils (1) to (8) Hydroisomerize the base oil or the lubricating oil fraction recovered from the base oil, and perform dewaxing treatment such as solvent dewaxing on the product or the lubricating oil fraction recovered from the product by distillation, Alternatively, hydroisomerized mineral oil obtained by distillation after the dewaxing treatment.

  Moreover, when obtaining the lubricating base oil of (9) or (10) above, a solvent refining treatment and / or a hydrofinishing treatment step may be further provided as necessary at a convenient step.

  The catalyst used for the hydrocracking / hydroisomerization is not particularly limited, but a composite oxide having cracking activity (for example, silica alumina, alumina boria, silica zirconia, etc.) or one of the composite oxides. Hydrogenolysis with a combination of the above combined with a binder and supporting a metal having hydrogenation ability (for example, one or more metals such as Group VIa metal or Group VIII metal in the periodic table) Hydroisomerization catalyst in which a catalyst or a support containing zeolite (for example, ZSM-5, zeolite beta, SAPO-11, etc.) is loaded with a metal having a hydrogenation ability containing at least one of Group VIII metals Are preferably used. The hydrocracking catalyst and the hydroisomerization catalyst may be used in combination by stacking or mixing.

The reaction conditions in the hydrocracking / hydroisomerization are not particularly limited, but the hydrogen partial pressure is 0.1 to 20 MPa, the average reaction temperature is 150 to 450 ° C., the LHSV is 0.1 to 3.0 hr ⁻¹ , the hydrogen / oil ratio. It is preferable to set it as 50-20000 scf / b.

  Preferable examples of the method for producing the lubricating base oil of the present invention include production method A shown below.

That is, the manufacturing method A according to the present invention includes:
NH ₃ to the carrier desorption of the fraction of the NH ₃ is 80% or less at 300 to 800 ° C. relative to the total desorption of NH ₃ in the desorption temperature dependence evaluation, at least one of the periodic table Group VIa metals And a first step of preparing a hydrocracking catalyst on which at least one of the Group VIII metals is supported,
In the presence of a hydrocracking catalyst, a feed oil containing 50% by volume or more of slack wax, hydrogen partial pressure 0.1-14 MPa, average reaction temperature 230-430 ° C., LHSV 0.3-3.0 hr ⁻¹ , hydrogen oil ratio A second step of hydrocracking at 50-14000 scf / b;
A third step of obtaining a lubricating oil fraction by distilling and separating the cracked product oil obtained in the second step;
And a fourth step of dewaxing the lubricating oil fraction obtained in the third step.

  Hereinafter, the production method A will be described in detail.

(Raw oil)
In the production method A, a raw material oil containing 50% by volume or more of slack wax is used. The “raw oil containing 50% by volume or more of slack wax” as used in the present invention is a mixed oil of a raw oil consisting only of slack wax, slack wax and other raw material oil, and 50 volumes of slack wax. % And both raw material oils containing at least% are included.

Slack wax is a wax-containing component by-produced in the solvent dewaxing step when producing a lubricating base oil from a paraffinic lubricating oil fraction. In the present invention, the slack wax is obtained by further deoiling the wax-containing component. Included in wax. The main components of slack wax are n-paraffins and branched paraffins (isoparaffins) with few side chains, and are low in naphthenes and aromatics. The kinematic viscosity of the slack wax used in the preparation of the raw material oil can be appropriately selected according to the kinematic viscosity of the target lubricating base oil, but a low viscosity base oil is produced as the lubricating base oil of the present invention. For this, a relatively low viscosity slack wax having a kinematic viscosity at 100 ° C. of about ² to 25 mm ² / s, preferably about 2.5 to ²⁰ mm ² / s, more preferably about 3 to 15 mm ² / s is desirable. . Moreover, although the other property of slack wax is also arbitrary, melting | fusing point becomes like this. Preferably it is 35-80 degreeC, More preferably, it is 45-70 degreeC, More preferably, it is 50-60 degreeC. The oil content of the slack wax is preferably 60% by mass or less, more preferably 50% by mass or less, further preferably 25% by mass or less, particularly preferably 10% by mass or less, and preferably 0.5% by mass. As mentioned above, More preferably, it is 1 mass% or more. The sulfur content of the slack wax is preferably 1% by mass or less, more preferably 0.5% by mass or less, and preferably 0.001% by mass or more.

  Here, the oil content of the fully deoiled slack wax (hereinafter referred to as “slack wax A”) is preferably 0.5 to 10% by mass, more preferably 1 to 8% by mass. The sulfur content of the slack wax A is preferably 0.001 to 0.2% by mass, more preferably 0.01 to 0.15% by mass, and still more preferably 0.05 to 0.12% by mass. On the other hand, the oil content of slack wax (hereinafter referred to as “slack wax B”) that is not deoiled or insufficiently deoiled is preferably 10 to 60% by mass, more preferably 12 to 50% by mass. More preferably, it is 15 to 25% by mass. The sulfur content of the slack wax B is preferably 0.05 to 1% by mass, more preferably 0.1 to 0.5% by mass, and still more preferably 0.15 to 0.25% by mass.

  In the production method A, by using the slack wax A as a raw material, it is possible to suitably obtain the lubricating base oil of the present invention that satisfies the conditions that the urea adduct value is 7% by mass or less and the viscosity index is 100 or more. Can do. In addition, according to the above production method A, even if slack wax B having a relatively high oil content and sulfur content, and relatively poor and inexpensive is used as a raw material, the viscosity index is high, and low temperature characteristics and thermal / oxidative stability are excellent. In addition, a lubricating base oil with high added value can be obtained.

  When the raw material oil is a mixed oil of slack wax and other raw material oil, the other raw material oil is not particularly limited as long as the ratio of slack wax to the total amount of the mixed oil is 50% by volume or more. A heavy oil-distilled distillate and / or a mixed oil of vacuum-distilled distillate is preferably used.

  Further, when the raw material oil is a mixed oil of slack wax and another raw material oil, the ratio of slack wax in the mixed oil is more preferably 70% by volume or more from the viewpoint of producing a base oil having a high viscosity index. 75% by volume or more is even more preferable. When the ratio is less than 50% by volume, the oil base such as aromatics and naphthenes in the obtained lubricating base oil tends to increase and the viscosity index of the lubricating base oil tends to decrease.

  On the other hand, the heavy atmospheric distillation distillate and / or vacuum distillation distillate of crude oil used in combination with slack wax has a distillation temperature of 300 to 570 ° C. in order to keep the viscosity index of the lubricating base oil produced high. A fraction having a distillate component of 60% by volume or more in the range is preferable.

(Hydrocracking catalyst)
In the manufacturing method A, the carrier desorption of the fraction of the NH ₃ is 80% or less at 300 to 800 ° C. relative to the total desorption of NH ₃ in the NH ₃ desorption temperature dependence evaluation, periodic table Group VIa A hydrocracking catalyst in which at least one of the metals and at least one of the Group VIII metals is supported is used.

Here, “NH ₃ desorption temperature dependency evaluation” refers to literature (Sawa M., Niwa M., Murakami Y., Zeolites 1990, 10, 532, Karge HG, Dondur V., J. Phys. Chem., 1990, 94, 765, etc.) and is performed as follows. First, the catalyst carrier is pretreated at a temperature of 400 ° C. or higher for 30 minutes or more under a nitrogen stream to remove adsorbed molecules, and then adsorbs NH ₃ at 100 ° C. until saturation. Then, the catalyst support to 100 to 800 ° C. 10 ° C. / min was heated by the following heating rate desorbed NH _3, to monitor the NH ₃ separated at every predetermined temperature by desorption. Then, the fraction of the NH ₃ desorption amount at 300 ° C. to 800 ° C. with respect to the total NH ₃ desorption amount (desorption amount at 100 to 800 ° C.) is obtained.

The catalyst carrier used in the manufacturing method A are those desorption of the fraction of NH ₃ at 300 to 800 ° C. relative to the total desorption of NH ₃ in the NH ₃ desorption temperature dependence evaluation of the following 80% , Preferably 70% or less, more preferably 60% or less. By constituting a hydrocracking catalyst using such a carrier, the acid properties that govern the cracking activity are sufficiently suppressed, so that the high molecular weight n-paraffin derived from slack wax or the like in the raw oil by hydrocracking. The production of isoparaffin by decomposition isomerization can be performed efficiently and reliably, and excessive decomposition of the produced isoparaffin compound can be sufficiently suppressed. As a result, a sufficient amount of molecules having a moderately branched chemical structure and a high viscosity index can be provided in an appropriate molecular weight range.

  As such a support, a binary oxide which is amorphous and has an acid property is preferable. For example, it is exemplified in the literature ("Metal oxide and its catalytic action", Tetsuro Shimizu, Kodansha, 1978). And binary oxides.

Among them, an amorphous composite oxide which is an acid composed of two kinds of oxides of elements selected from Al, B, Ba, Bi, Cd, Ga, La, Mg, Si, Ti, W, Y, Zn and Zr. It is preferable to contain a property binary oxide. By adjusting the ratio of each oxide of these acid property binary oxides, a support having an acid property suitable for this purpose can be obtained in the NH ₃ adsorption / desorption evaluation. In addition, the acid property binary oxide constituting the carrier may be one of the above or a mixture of two or more. Further, the carrier may be composed of the above-mentioned acid property binary oxide, or may be a carrier obtained by binding the acid property binary oxide with a binder.

  Further, the carrier is amorphous silica / alumina, amorphous silica / zirconia, amorphous silica / magnesia, amorphous silica / titania, amorphous silica / boria, amorphous alumina / zirconia, amorphous alumina / magnesia, amorphous At least one selected from alumina / titania, amorphous alumina / boria, amorphous zirconia / magnesia, amorphous zirconia / titania, amorphous zirconia / boria, amorphous magnesia / titania, amorphous magnesia / boria and amorphous titania / boria It is preferable to contain two kinds of acid nature binary oxides. The acidic binary oxide constituting the carrier may be one of the above or a mixture of two or more. Further, the carrier may be composed of the above-mentioned acid property binary oxide, or may be a carrier obtained by binding the acid property binary oxide with a binder. The binder is not particularly limited as long as it is generally used for catalyst preparation, but is preferably selected from silica, alumina, magnesia, titania, zirconia, clay, or a mixture thereof.

  In the production method A described above, the carrier is composed of at least one of group VIa metals (molybdenum, chromium, tungsten, etc.) of the periodic table and group VIII metal (nickel, cobalt, palladium, platinum, etc.). At least one of them is supported to form a hydrocracking catalyst. These metals are responsible for hydrogenation ability, terminate the reaction in which the paraffinic compound is decomposed or branched by the acidic carrier, and play an important role in producing isoparaffin having an appropriate molecular weight and branched structure.

  As the amount of metal supported in the hydrocracking catalyst, the supported amount of Group VIa metal is 5 to 30% by mass per one type of metal, and the supported amount of Group VIII metal is 0.2 to 10% by mass per one type of metal. % Is preferred.

  Further, in the hydrocracking catalyst used in the production method A, molybdenum is contained in the range of 5 to 30% by mass as one or more metals of the Group VIa metal, and one or more of the Group VIII metals is contained. More preferably, the metal contains nickel in the range of 0.2 to 10% by mass.

  The hydrocracking catalyst composed of the above support and one or more metals of Group VIa metal and one or more metals of Group VIII metal is preferably used for hydrocracking in a sulfurized state. The sulfurization treatment can be performed by a known method.

(Hydrolysis process)
In the production method A, a raw material oil containing 50% by volume or more of slack wax in the presence of the hydrocracking catalyst has a hydrogen partial pressure of 0.1 to 14 MPa, preferably 1 to 14 MPa, more preferably 2 to 2. 7 MPa; average reaction temperature of 230 to 430 ° C., preferably 330 to 400 ° C., more preferably 350 to 390 ° C .; LHSV of 0.3 to 3.0 hr ⁻¹ , preferably 0.5 to 2.0 hr ⁻¹ ; Hydrogenolysis is performed at a hydrogen oil ratio of 50 to 14,000 scf / b, preferably 100 to 5000 scf / b.

  In such a hydrocracking process, isomerization to isoparaffin progresses in the process of cracking n-paraffin derived from slack wax in the raw material oil, thereby producing an isoparaffin component having a low pour point and a high viscosity index. At the same time, it breaks down aromatic compounds, which are inhibitors of high viscosity index contained in the feedstock, into monocyclic aromatic compounds, naphthene compounds and paraffin compounds, and inhibits high viscosity index. The polycyclic naphthene compound as a factor can be decomposed into a monocyclic naphthene compound or a paraffin compound. From the viewpoint of increasing the viscosity index, it is preferable that the raw material oil contains fewer compounds having a high boiling point and a low viscosity index.

Further, the decomposition rate for evaluating the progress of the reaction is expressed by the following formula:
(Decomposition rate (volume%)) = 100− (ratio of the fraction having a boiling point of 360 ° C. or more in the product (volume%))
In this way, the decomposition rate is preferably 3 to 90% by volume. When the decomposition rate is less than 3% by volume, isoparaffins are generated by decomposition and isomerization of high-molecular-weight n-paraffins having a high pour point contained in the feedstock, and hydrocracking of aromatics and polycyclic naphthenes with poor viscosity index. When the decomposition rate exceeds 90% by volume, the yield of the lubricating oil fraction decreases, which is not preferable.

(Distillation separation process)
Next, the lubricating oil fraction is distilled and separated from the cracked product oil obtained by the hydrocracking step. At this time, a fuel oil fraction may be obtained as a light component.

  The fuel oil fraction is a fraction obtained as a result of sufficient desulfurization and denitrogenation, and sufficient aromatic hydrogenation. Among these, the naphtha fraction has a high isoparaffin content, the kerosene fraction has a high smoke point, and the light oil fraction has a high cetane number.

  On the other hand, when hydrocracking in the lubricating oil fraction is insufficient, a part of it may be subjected to the hydrocracking process again. Further, in order to obtain a lubricating oil fraction having a desired kinematic viscosity, the lubricating oil fraction may be further distilled under reduced pressure. This vacuum distillation separation may be performed after the dewaxing treatment described below.

  In the evaporative separation step, a lubricant base oil called 70 Pale, SAE10, or SAE20 can be suitably obtained by distilling the cracked product oil obtained in the hydrocracking step under reduced pressure.

  A system that uses slack wax with lower viscosity as the feedstock is suitable for producing a large amount of 70 Pale and 10 SAE fractions, and a system that uses slack wax with a high viscosity within the above range as feedstock produces a lot of SAE20. Suitable for doing. However, even if a high-viscosity slack wax is used, conditions for generating a considerable amount of 70 Pale and SAE 10 can be selected depending on the progress of the decomposition reaction.

(Dewaxing process)
In the above-described distillation separation step, since the lubricating oil fraction fractionated from the cracked product oil has a high pour point, it is dewaxed to obtain a lubricating base oil having a desired pour point. The dewaxing treatment can be performed by a usual method such as a solvent dewaxing method. Among these, the solvent dewaxing method generally uses a mixed solvent of MEK and toluene, but may use a solvent such as benzene, acetone, MIBK or the like. In order to make the pour point of the dewaxed oil not more than −10 ° C., the solvent / oil ratio is 1 to 6 times and the filtration temperature is −5 to −45 ° C., preferably −10 to −40 ° C. The wax removed here can be used again as a slack wax in the hydrocracking step.

  In the said manufacturing method, you may add a solvent refinement | purification process and / or a hydrorefining process to a dewaxing process. These additional treatments are performed in order to improve the ultraviolet stability and oxidation stability of the lubricating base oil, and can be carried out by a method used in a normal lubricating oil refining process.

  In the solvent purification, furfural, phenol, N-methylpyrrolidone or the like is generally used as a solvent, and a small amount of aromatic compounds, particularly polycyclic aromatic compounds remaining in the lubricating oil fraction are removed.

In addition, hydrorefining is performed to hydrogenate olefin compounds and aromatic compounds, and the catalyst is not particularly limited. However, at least one of Group VIa metals such as molybdenum, cobalt, nickel, etc. Using an alumina catalyst supporting at least one of the Group VIII metals, the reaction pressure (hydrogen partial pressure) is 7 to 16 MPa, the average reaction temperature is 300 to 390 ° C., and the LHSV is 0.5 to 4.0 hr ⁻¹ . Can be done below.

  Moreover, as a preferable example of the method for producing the lubricating base oil of the present invention, the following production method B can be mentioned.

That is, the production method B according to the present invention is:
A fifth step of hydrocracking a feedstock containing paraffinic hydrocarbons in the presence of a catalyst;
A sixth step of dewaxing the product obtained in the fifth step or the lubricating oil fraction recovered from the product by distillation or the like;
Is provided.

  Hereinafter, the production method B will be described in detail.

(Raw oil)
In the production method B, a raw material oil containing paraffinic hydrocarbon is used. The “paraffinic hydrocarbon” referred to in the present invention means a hydrocarbon having a paraffin molecule content of 70% by mass or more. The carbon number of the paraffinic hydrocarbon is not particularly limited, but usually about 10 to 100 is used. The paraffinic hydrocarbon production method is not particularly limited, and various paraffinic hydrocarbons such as petroleum and synthetic can be used. Particularly preferable paraffinic hydrocarbons include a gas-liquid (GTL) process and the like. Synthetic waxes obtained (Fischer-Tropsch wax (FT wax), GTL wax, etc.) can be mentioned, among which FT wax is preferred. The synthetic wax is preferably a wax containing, as a main component, a normal paraffin having 15 to 80 carbon atoms, more preferably 20 to 50 carbon atoms.

The kinematic viscosity of the paraffinic hydrocarbon used in the preparation of the raw material oil can be appropriately selected according to the kinematic viscosity of the target lubricating base oil, but a low viscosity base oil is used as the lubricating base oil of the present invention. For production, a relatively low-viscosity paraffinic system having a kinematic viscosity at 100 ° C. of about ² to 25 mm ² / s, preferably about 2.5 to ²⁰ mm ² / s, more preferably about 3 to 15 mm ² / s. Hydrocarbons are desirable. In addition, other properties of the paraffinic hydrocarbon are optional, but when the paraffinic hydrocarbon is a synthetic wax such as FT wax, the melting point is preferably 35 to 80 ° C, more preferably 50 to 80 ° C, More preferably, it is 60-80 degreeC. The oil content of the synthetic wax is preferably 10% by mass or less, more preferably 5% by mass or less, and further preferably 2% by mass or less. The sulfur content of the synthetic wax is preferably 0.01% by mass or less, more preferably 0.001% by mass or less, and further preferably 0.0001% by mass or less.

  When the raw material oil is a mixed oil of the above synthetic wax and another raw material oil, the other raw material oil is not particularly limited as long as the ratio of the synthetic wax to the total amount of the mixed oil is 50% by volume or more. A heavy atmospheric distillation oil and / or a mixed oil of reduced pressure distillation oil is preferably used.

  Further, when the raw material oil is a mixed oil of the above synthetic wax and other raw material oils, the proportion of the synthetic wax in the mixed oil is more than 70% by volume from the viewpoint of producing a base oil having a high viscosity index. Preferably, 75% by volume or more is even more preferable. If the ratio is less than 70% by volume, the lubricating base oil to be obtained tends to increase the oil content such as aromatics and naphthenes and decrease the viscosity index of the lubricating base oil.

  On the other hand, heavy crude pressure distillation distillate and / or vacuum distillation distillate of crude oil used in combination with synthetic wax is used at a distillation temperature of 300 to 570 ° C. in order to keep the viscosity index of the lubricating base oil to be produced high. A fraction having a distillate component of 60% by volume or more in the range is preferable.

(catalyst)
The catalyst used in production method B is not particularly limited, but a catalyst in which at least one selected from Group VI metal and Group VIII metal of the periodic table as an active metal component is supported on a support containing aluminosilicate. Preferably used.

  Aluminosilicate refers to a metal oxide composed of three elements of aluminum, silicon, and oxygen. Further, other metal elements can be allowed to coexist within a range that does not hinder the effects of the present invention. In this case, the amount of the other metal element is preferably 5% by mass or less, and more preferably 3% by mass or less of the total amount of alumina and silica as the oxide. Examples of metal elements that can coexist include titanium, lanthanum, manganese, and the like.

The crystallinity of aluminosilicate can be estimated by the proportion of tetracoordinate aluminum atoms in all aluminum atoms, and this proportion can be measured by ²⁷ Al solid state NMR. As the aluminosilicate used in the present invention, the ratio of tetracoordinated aluminum to the total amount of aluminum is preferably 50% by mass or more, more preferably 70% by mass or more, and further preferably 80% by mass or more. Hereinafter, an aluminosilicate in which the ratio of tetracoordinated aluminum to the total amount of aluminum is 50% by mass or more is referred to as “crystalline aluminosilicate”.

  As the crystalline aluminosilicate, so-called zeolite can be used. Preferable examples include Y-type zeolite, ultra-stable Y-type zeolite (USY-type zeolite), β-type zeolite, mordenite, ZSM-5, etc. Among them, USY zeolite is particularly preferable. In the present invention, one type of crystalline aluminosilicate may be used alone, or two or more types may be used in combination.

  Examples of a method for preparing a carrier containing crystalline aluminosilicate include a method of molding a mixture of crystalline aluminosilicate and a binder and firing the molded body. The binder to be used is not particularly limited, but alumina, silica, silica alumina, titania and magnesia are preferable, and alumina is particularly preferable. The use ratio of the binder is not particularly limited, but is usually preferably 5 to 99% by mass and more preferably 20 to 99% by mass based on the total amount of the molded body. 430-470 degreeC is preferable, as for the baking temperature of the molded object containing a crystalline aluminosilicate and a binder, 440-460 degreeC is more preferable, and 445-455 degreeC is more preferable. The firing time is not particularly limited, but is usually 1 minute to 24 hours, preferably 10 minutes to 20 hours, more preferably 30 minutes to 10 hours. Firing may be performed in an air atmosphere, but is preferably performed in an oxygen-free atmosphere such as a nitrogen atmosphere.

  Examples of the Group VI b metal supported on the carrier include chromium, molybdenum, tungsten, and the like. Specific examples of the Group VIII metal include cobalt, nickel, rhodium, palladium, iridium, platinum, and the like. It is done. These metals may be used individually by 1 type, or may be used in combination of 2 or more types. When two or more kinds of metals are combined, noble metals such as platinum and palladium may be combined, base metals such as nickel, cobalt, tungsten and molybdenum may be combined, or a noble metal and a base metal may be combined.

  Further, the loading of the metal on the carrier can be performed by information such as impregnation of the carrier into a solution containing the metal, ion exchange, and the like. The amount of the metal supported can be appropriately selected, but is usually 0.05 to 2% by mass, preferably 0.1 to 1% by mass based on the total amount of the catalyst.

(Hydrolysis process)
In the production method B, the raw material oil containing paraffinic hydrocarbon is hydrocracked in the presence of the catalyst. Such a hydrocracking step can be performed using a fixed bed reactor. As hydrocracking conditions, for example, the temperature is preferably 250 to 400 ° C., the hydrogen pressure is preferably 0.5 to 10 MPa, and the liquid space velocity (LHSV) of the raw material oil is preferably 0.5 to 10 h ⁻¹ .

(Distillation separation process)
Next, the lubricating oil fraction is distilled and separated from the cracked product oil obtained by the hydrocracking step. In addition, since the distillation separation process in the manufacturing method B is the same as the distillation separation process in the manufacturing method A, the overlapping description is abbreviate | omitted here.

(Dewaxing process)
Subsequently, the lubricating oil fraction fractionated from the cracked product oil in the distillation separation step is dewaxed. Such a dewaxing step can be performed using a conventionally known dewaxing process such as solvent dewaxing. Here, if the substance having a boiling point of 370 ° C. or less present in the cracked product oil is not separated from the high boiling point material prior to dewaxing, the total hydroisomerized product may be dewaxed depending on the use of the cracked product oil. Alternatively, a fraction having a boiling point of 370 ° C. or higher may be removed.

  In solvent dewaxing, the hydroisomerized product is contacted with chilled ketone and acetone, and other solvents such as MEK, MIBK, and further cooled to precipitate the high pour point material as a waxy solid, which is precipitated with raffinate. Separate from a solvent-containing lubricating oil fraction. Further, the raffinate can be cooled with a scraped surface chiller to remove wax solids. Also, low molecular weight hydrocarbons such as propane can be used for dewaxing. In this case, cracked oil and low molecular weight hydrocarbon are mixed, and at least a part thereof is vaporized to further cool the cracked product oil. To precipitate the wax. The wax is separated from the raffinate by filtration, membrane or centrifugation. Thereafter, the solvent is removed from the raffinate, and the raffinate is fractionally distilled to obtain the target lubricating base oil.

  As mentioned above, although the manufacturing method A and the manufacturing method B which are the preferable manufacturing methods of the lubricating base oil of this invention were demonstrated, the manufacturing method of the lubricating base oil of this invention is not limited to these. For example, in the above production method A, synthetic waxes such as FT wax and GTL wax may be used instead of slack wax. In the production method B, a raw material oil containing slack wax (preferably slack wax A, B) may be used. Furthermore, in each of the production methods A and B, slack wax (preferably slack wax A and B) and synthetic wax (preferably FT wax and GTL wax) may be used in combination.

  In addition, when the raw material oil used when producing the lubricating base oil of the present invention is a mixed oil of the above slack wax and / or synthetic wax and a raw material oil other than these waxes, slack wax and The content of the synthetic wax is preferably 50% by mass or more based on the total amount of the raw material oil.

  Further, when producing a lubricating base oil satisfying the condition that the urea adduct value is 7% by mass or less and the viscosity index is 100 or more, the raw material oil is a raw material oil containing slack wax and / or synthetic wax. A raw material oil having an oil content of 0 to 60% by mass, preferably 10 to 50% by mass is preferred; a raw material oil containing slack wax A and / or slack wax B, wherein the oil content is 0.5 to 60% More preferred is a feedstock having a mass%, preferably 10 to 50; particularly preferred is a feedstock containing slack wax B and having an oil content of 5 to 60 mass, preferably 10 to 50 mass%.

  Further, when the lubricating base oil of the present invention satisfies the condition that the urea adduct value is 7% by mass or less and the viscosity index is 100 or more, the saturated content in the lubricating base oil Based on the total amount of the base oil, it is 90% by mass or more as described above, preferably 95% by mass or more, more preferably 96% by mass or more, and still more preferably 97% by mass or more. Moreover, the ratio of the cyclic | annular saturated part which occupies for the said saturated part is 10-40 mass% as above-mentioned, Preferably it is 10.5-30 mass%, More preferably, it is 11-25 mass%, More preferably, it is 12-21. % By mass. Viscosity-temperature characteristics and thermal / oxidative stability can be achieved by satisfying the above conditions for the content of the saturated component and the ratio of the cyclic saturated component in the saturated component, respectively. When the additive is blended, the function of the additive can be expressed at a higher level while the additive is sufficiently stably dissolved and held in the lubricating base oil. Furthermore, when the content of the saturated component and the ratio of the cyclic saturated component in the saturated component satisfy the above conditions, the friction characteristics of the lubricating base oil itself can be improved, and as a result, the friction reducing effect is improved. As a result, energy saving can be improved.

  If the saturated content is less than 90% by mass, the viscosity-temperature characteristics, thermal / oxidation stability, and friction characteristics will be insufficient. Further, when the ratio of the cyclic saturated component to the saturated component is less than 10% by mass, when the additive is blended with the lubricating base oil, the solubility of the additive may be insufficient, Since the effective amount of the additive dissolved and retained in the oil base oil is reduced, the function of the additive cannot be effectively obtained. Furthermore, when the ratio of the cyclic saturated component in the saturated component exceeds 40% by mass, the effectiveness of the additive is reduced when the additive is blended with the lubricating base oil. Further, the content of the saturated component may be 100% by mass, but is preferably 99.9% by mass or less, more preferably 99.5% by mass or less, from the viewpoint of reducing the production cost and improving the solubility of the additive. More preferably, it is 99 mass% or less, Most preferably, it is 98.5 mass% or less.

  When the lubricating base oil of the present invention satisfies the condition that the urea adduct value is 7% by mass or less and the viscosity index is 100 or more, the ratio of the cyclic saturated component to the saturated component is 10 to 40% by mass. It is equivalent that the non-cyclic saturated component in the saturated component is 60 to 90% by mass. Here, the non-cyclic saturated component includes both a linear paraffin component and a branched paraffin component. The proportion of each paraffin component in the lubricating base oil of the present invention is not particularly limited, but the proportion of the branched paraffin component is preferably 55 to 99 mass%, more preferably 57.5 based on the total amount of the lubricating oil base oil. It is -95 mass%, More preferably, it is 60-95 mass%, More preferably, it is 70-90 mass%, Most preferably, it is 80-90 mass%. When the ratio of the branched paraffin content in the lubricating base oil satisfies the above conditions, the viscosity-temperature characteristics and thermal / oxidative stability can be further improved, and an additive is added to the lubricating base oil. In this case, the function of the additive can be expressed at a higher level while the additive is sufficiently stably dissolved and held.

  In addition, content of the saturated part said by this invention means the value (unit: mass%) measured based on ASTM D 2007-93.

  Moreover, the ratio of the cyclic saturated component and the non-cyclic saturated component in the saturated component referred to in the present invention is a naphthene component measured according to ASTM D 2786-91, respectively (measuring object: 1-ring to 6-ring naphthene, unit : Mass%) and alkane content (unit: mass%).

In addition, the linear paraffin content in the lubricating base oil referred to in the present invention is the gas chromatographic analysis of the saturated content separated and separated by the method described in ASTM D 2007-93 under the following conditions. The value obtained by converting the measured value when the linear paraffin content in the saturated content is identified and quantified based on the total amount of the lubricating base oil is meant. In the identification and quantification, a mixed sample of straight-chain paraffin having 5 to 50 carbon atoms is used as a standard sample, and the straight-chain paraffin content in the saturated portion is the total peak area value of the chromatogram (in the diluent). It is determined as the ratio of the sum of peak area values corresponding to each linear paraffin to (excluding the peak area value derived from).
(Gas chromatography conditions)
Column: non-polar liquid phase column (length 25 mm, inner diameter 0.3 mmφ, liquid phase film thickness 0.1 μm)
Temperature rising condition: 50 ° C. to 400 ° C. (temperature rising rate: 10 ° C./min)
Carrier gas: helium (linear velocity: 40 cm / min)
Split ratio: 90/1
Sample injection amount: 0.5 μL (injection amount of sample diluted 20 times with carbon disulfide)

  The ratio of branched paraffin in the lubricating base oil is the difference between the non-cyclic saturated content in the saturated content and the linear paraffin content in the saturated content, converted based on the total amount of the lubricating base oil. Means the value.

  In the case of a method for separating saturated components, or a compositional analysis of cyclic saturated components, non-cyclic saturated components, etc., a similar method can be used in which similar results can be obtained. For example, in addition to the above, a method described in ASTM D 2425-93, a method described in ASTM D 2549-91, a method using high performance liquid chromatography (HPLC), a method obtained by improving these methods, and the like can be given.

  The aromatic content in the lubricating base oil of the present invention is not particularly limited as long as the lubricating base oil satisfies the condition that the urea adduct value is 7% by mass or less and the viscosity index is 100 or more. On the basis of the total amount of the oil base oil, preferably 10% by mass or less, more preferably 0.1 to 5% by mass, still more preferably 0.2 to 4.5% by mass, particularly preferably 0.3 to 3% by mass. is there. If the aromatic content exceeds the above upper limit, the viscosity-temperature characteristics, thermal / oxidative stability, friction characteristics, volatilization prevention characteristics and low-temperature viscosity characteristics tend to decrease. When an additive is blended with the additive, the effectiveness of the additive tends to decrease. Further, the lubricating base oil of the present invention may not contain an aromatic component, but the solubility of the additive can be further improved by setting the aromatic content to be equal to or higher than the above lower limit value. it can.

  In addition, content of an aromatic content here means the value measured based on ASTM D 2007-93. In general, the aromatic component includes alkylbenzene, alkylnaphthalene, anthracene, phenanthrene and alkylated products thereof, as well as compounds in which four or more benzene rings are condensed, pyridines, quinolines, phenols and naphthols. Aromatic compounds having atoms are included.

Further, the% C _p of the lubricating base oil of the present invention is not particularly limited as long as the lubricating base oil satisfies the above condition that the condition urea adduct value is 7 mass% or less and the viscosity index is 100 or more. , Preferably 80 or more, more preferably 82 to 99, still more preferably 85 to 95, particularly preferably 87 to 93. When% C _p of lubricating base oil is less than the above lower limit, viscosity-temperature characteristics, thermal / oxidative stability, and friction characteristics tend to decrease, and further, additives are added to lubricating base oil In addition, the effectiveness of the additive tends to decrease. Further, when the% C _p value of the lubricating base oil exceeds the upper limit value, the additive solubility will tend to be lower.

Moreover,% C _N of the lubricating base oil of the invention is a lubricating base oil is at the urea adduct value is 7 wt% or less and a viscosity index is not particularly limited so long as it satisfies the condition of 100 or more, preferably Is 19 or less, more preferably 5 to 15, still more preferably 7 to 13, particularly preferably 8 to 12. If the% C _N value of the lubricating base oil exceeds the upper limit value, the viscosity - temperature characteristic, heat and oxidation stability and frictional properties will tend to be reduced. Moreover, when% _CN is less than the said lower limit, it exists in the tendency for the solubility of an additive to fall.

Moreover,% C _A of the lubricating base oil of the invention is and viscosity index is a urea adduct value is 7 mass% or less is not particularly limited so long as it satisfies the condition of 100 or more, preferably 5 or less, more Preferably it is 2 or less, more preferably 1.5 or less, particularly preferably 1 or less. When% C _A of the lubricating base oil exceeds the upper limit value, the viscosity - temperature characteristic, heat and oxidation stability and frictional properties will tend to be reduced. Moreover,% C _A of the lubricating base oil of the invention may be 0% by 0.1 or more C _A, it is possible to further increase the solubility of additives.

Furthermore, the ratio of the percentages in the lubricating base oil C _P and% C _N of the present invention, the lubricating oil base oil is not greater than the urea adduct value is 7% by mass and a viscosity index satisfies the condition of more than 100 it is not particularly limited as long as,% C is preferably P _/% C _N is 5 or more, more preferably 6 or more, more preferably 7 or more. When% C _P /% _CN is less than the above lower limit value, viscosity-temperature characteristics, thermal / oxidative stability and friction characteristics tend to decrease, and further, when an additive is blended in the lubricating base oil In addition, the effectiveness of the additive tends to decrease. _{Moreover,% C} P /% C _N is preferably 35 or less, more preferably 20 or less, further preferably 14 or less, and particularly preferably 13 or less. % Of C P _/% C _N by the above-described upper limit or less, it is possible to further increase the solubility of additives.

Incidentally, _say% C P in the present invention,% _C A _N and% _{C A,} obtained by a method in accordance with ASTM D 3238-85, respectively (n-d-M ring analysis), the total carbon number of the paraffin carbon number The percentage of the total number of naphthene carbons to the total number of carbons, and the percentage of the total number of aromatic carbons to the total number of carbons. That is, the preferred ranges of% C _P ,% C _N and% C _A described above are based on the values obtained by the above method. For example, even a lubricating base oil containing no naphthene is obtained by the above method. is% C _N may indicate a value greater than zero.

  Further, the sulfur content in the lubricating base oil of the present invention depends on the sulfur content of the raw material. For example, when a raw material that does not substantially contain sulfur such as a synthetic wax component obtained by a Fischer-Tropsch reaction or the like is used, a lubricating base oil that does not substantially contain sulfur can be obtained. In addition, when using raw materials containing sulfur such as slack wax obtained in the refining process of the lubricating base oil and microwax obtained in the refining process, the sulfur content in the obtained lubricating base oil is usually 100 mass ppm. That's it. In the lubricating base oil of the present invention, the content of sulfur is preferably 100 mass ppm or less, more preferably 50 mass ppm or less, from the viewpoint of further improving thermal and oxidation stability and reducing sulfur content. Is more preferably 10 ppm by mass or less, and particularly preferably 5 ppm by mass or less.

  Further, from the viewpoint of cost reduction, it is preferable to use slack wax or the like as a raw material. In that case, the sulfur content in the obtained lubricating base oil is preferably 50 ppm by mass or less, and preferably 10 ppm by mass or less. More preferred. In addition, the sulfur content as used in the field of this invention means the sulfur content measured based on JISK2541-1996.

  Further, the nitrogen content in the lubricating base oil of the present invention is not particularly limited, but is preferably 5 ppm by mass or less, more preferably 3 ppm by mass or less, and further preferably 1 ppm by mass or less. If the nitrogen content exceeds 5 ppm by mass, the thermal and oxidation stability tends to decrease. In addition, the nitrogen content as used in the field of this invention means the nitrogen content measured based on JISK2609-1990.

The kinematic viscosity of the lubricating base oil of the present invention is not particularly limited as long as the lubricating base oil satisfies the condition that the urea adduct value is 7% by mass or less and the viscosity index is 100 or more. The kinematic viscosity at ° C. is preferably 2.5 to 10.0 mm ² / s, more preferably 2.8 to 8.0, still more preferably 3.1 to 7.0 mm ² / s, and particularly preferably 3.4. -6.0 mm < ² > / s. When the kinematic viscosity at 100 ° C. of the lubricating base oil is less than 2.5 mm ² / s, it is not preferable in terms of evaporation loss. Moreover, when it is going to obtain the lubricating base oil whose kinematic viscosity in 100 degreeC exceeds 10.0 mm < ² > / s, the yield becomes low, and even when it is a case where heavy wax is used as a raw material, a decomposition rate is raised. This is not preferable because it becomes difficult.

In the present invention, it is preferable to use a lubricating base oil having a kinematic viscosity at 100 ° C. in the following range by distillation or the like.
(I) less than the kinematic viscosity at 100 ° C. is 1.5 mm ² / s or more 3.5 mm ² / s, more preferably kinematic viscosity at 2.0 to 3.0 mm ² / s lubricating base oils (II) 100 ° C. There 3.0 mm ² / s or more 4.5mm less than ² / s, more preferably a kinematic viscosity at 3.5~4.1mm ² / s lubricating base oil (III) 100 ℃ 4.5~20mm ² / s, more preferably 4.8 to 11 mm ² / s, particularly preferably 5.5 to 8.0 mm ² / s.

The kinematic viscosity at 40 ° C. of the lubricating base oil of the present invention is preferably 10 to 26 mm ² / s, more preferably 11 to 24 mm ² / s, still more preferably 12 to 22 mm ² / s, and particularly preferably 13 ˜20 mm ² / s. When the kinematic viscosity at 40 ° C. is less than 10 mm ² / s, there is a possibility that problems may occur in oil film retention and evaporability at the lubrication site. Moreover, when the kinematic viscosity at 40 ° C. is 26 mm ² / s or more, the low temperature viscosity characteristics may be deteriorated, which is not preferable. In the present invention, it is preferred that a lubricating oil fraction having a kinematic viscosity at 40 ° C. in the following range is fractionated by distillation or the like and used.
(IV) less than the kinematic viscosity at 40 ° C. is 6.0 mm ² / s or more 12 mm ² / s, more preferably 8.0~12mm ² / s lubricating base oil (V) kinematic viscosity at 40 ° C. is 12 mm ² / More than s and less than 28 mm < ² > / s, more preferably 13-19 mm < ² > / s lubricating base oil (VI) The kinematic viscosity at 40 [deg.] C. is 28-50 mm < ² > / s, more preferably 29-45 mm < ² > / s, particularly preferred. Is a lubricating base oil of 30 to 40 mm ² / s.

  The above lubricating base oils (I) and (IV) have a urea adduct value of 7% by mass or less and a viscosity index of 100 or more, so that compared with conventional lubricating base oils having the same viscosity grade. In particular, the low-temperature viscosity characteristics are excellent, and the viscosity resistance and stirring resistance can be remarkably reduced. Moreover, the BF viscosity in -40 degreeC can be 2000 mPa * s or less by mix | blending a pour point depressant. The BF viscosity at −40 ° C. means the viscosity measured according to JPI-5S-26-99.

  The lubricating base oils (II) and (V) have a urea adduct value of 7% by mass or less and a viscosity index of 100 or more. In comparison, it is particularly excellent in low-temperature viscosity characteristics, volatilization prevention properties and lubricity. For example, in the lubricating base oils (II) and (V), the CCS viscosity at −35 ° C. can be set to 3000 mPa · s or less.

  The lubricating base oils (III) and (VI) have a urea adduct value of 7% by mass or less and a viscosity index of 100 or more. In comparison, it has excellent low-temperature viscosity characteristics, volatilization prevention properties, thermal / oxidation stability, and lubricity.

  The viscosity index of the lubricating base oil of the present invention depends on the viscosity grade of the lubricating base oil, but needs to be 100 or more. For example, the viscosity index of the lubricating oils (I) and (IV) is , Preferably 105 to 130, more preferably 110 to 125, still more preferably 120 to 125. The viscosity index of the lubricating base oils (II) and (V) is preferably 125 to 160, more preferably 130 to 150, and still more preferably 135 to 150. Further, the viscosity index of the lubricating base oils (III) and (VI) is preferably 135 to 180, more preferably 140 to 160. When the viscosity index is less than the lower limit, viscosity-temperature characteristics, thermal / oxidation stability, and further volatilization prevention properties tend to decrease. On the other hand, when the viscosity index exceeds the upper limit, the low-temperature viscosity characteristics tend to decrease.

  Further, the CCS viscosity of the lubricating base oil of the present invention at −35 ° C. depends on the viscosity grade of the lubricating base oil. For example, the CCS of the lubricating base oil (I) and (IV) at −35 ° C. The viscosity is preferably 1000 mPa · s or less. The CCS viscosity at −35 ° C. of the lubricating base oils (II) and (V) is preferably 3000 mPa · s or less, more preferably 2400 mPa · s or less, still more preferably 2200 mPa · s or less, and particularly preferably 2000 mPa · s. -S or less. Further, the CCS viscosity of the lubricating base oils (III) and (VI) at −35 ° C. is preferably 15000 mPa · s or less, more preferably 10000 mPa · s or less, and further preferably 8000 mPa · s or less. When the CCS viscosity at −35 ° C. exceeds the upper limit, the low-temperature fluidity of the entire lubricating oil using the lubricating base oil tends to decrease. In addition, the CCS viscosity at −35 ° C. in the present invention means a viscosity measured according to JIS K 2010-1993.

  The MRV viscosity of the lubricating base oil of the present invention at −40 ° C. depends on the viscosity grade of the lubricating base oil. For example, the MRV of the lubricating base oils (I) and (IV) at −40 ° C. The viscosity is preferably 10,000 mPa · s or less. The MRV viscosity at −40 ° C. of the lubricating base oils (II) and (V) is preferably 60000 mPa · s or less, more preferably 40000 mPa · s or less, still more preferably 30000 mPa · s or less, and particularly preferably 25000 mPas. -S or less. Further, the MRV viscosity at −40 ° C. of the lubricating base oils (III) and (VI) is preferably 60000 mPa · s or less, more preferably 50000 mPa · s or less, and further preferably 40000 mPa · s or less. When the MRV viscosity at −40 ° C. exceeds the upper limit, the low temperature fluidity of the whole lubricating oil using the lubricating base oil tends to be lowered. The MRV viscosity at −40 ° C. in the present invention means a viscosity measured according to JPI-5S-42-93.

  Further, the pour point of the lubricating base oil of the present invention depends on the viscosity grade of the lubricating base oil. For example, the pour point of the lubricating base oils (I) and (IV) is preferably -10 ° C. Hereinafter, it is more preferably −12.5 ° C. or less, and further preferably −15 ° C. or less. The pour points of the lubricating base oils (II) and (V) are preferably −10 ° C. or lower, more preferably −15 ° C. or lower, and still more preferably −17.5 ° C. or lower. The pour point of the lubricating base oils (III) and (VI) is preferably −10 ° C. or lower, more preferably −12.5 ° C. or lower, and still more preferably −15 ° C. or lower. When the pour point exceeds the upper limit, the low temperature fluidity of the entire lubricating oil using the lubricating base oil tends to decrease. In addition, the pour point as used in the field of this invention means the pour point measured based on JISK2269-1987.

  Further, the refractive index at 20 ° C. of the lubricating base oil of the present invention depends on the viscosity grade of the lubricating base oil. For example, the refractive index at 20 ° C. of the lubricating base oils (I) and (IV) is , Preferably 1.440 to 1.460, more preferably 1.442 to 1.458, and still more preferably 1.445 to 1.455. Moreover, the refractive index at 20 ° C. of the lubricating base oils (II) and (V) is preferably 1.450 to 1.465, more preferably 1.452 to 1.460, still more preferably 1.453 to 1.458. Further, the refractive index of the lubricating base oils (III) and (VI) at 20 ° C. is preferably 1.455 to 1.468, more preferably 1.458 to 1.466, and still more preferably 1.457 to 1.465. If the refractive index exceeds the above upper limit, the viscosity-temperature characteristics and thermal / oxidative stability of the lubricating base oil tend to be reduced, and further, the volatilization preventing properties and low-temperature viscosity characteristics tend to deteriorate. When an additive is blended with the additive, the effectiveness of the additive tends to decrease.

Further, the density (ρ ₁₅ , unit: g / cm ³ ) of the lubricating base oil of the present invention at 15 ° C. depends on the viscosity grade of the lubricating base oil, but is not more than the value of ρ represented by the following formula (2). That is, it is preferable that ρ ₁₅ ≦ ρ.
ρ = 0.0025 × kv100 + 0.820 (2)
[Wherein, kv100 represents the kinematic viscosity (mm ² / s) of the lubricating base oil at 100 ° C. ]

When ρ ₁₅ > ρ, the viscosity-temperature characteristics and thermal / oxidation stability, volatilization prevention properties and low-temperature viscosity characteristics tend to decrease, and additives are added to the lubricating base oil. In some cases, the effectiveness of the additive tends to decrease.

For example, ρ ₁₅ of the lubricating base oils (I) and (IV) is preferably 0.830 g / cm ³ or less, more preferably 0.825 g / cm ³ or less, and still more preferably 0.820 g / cm ³ or less. It is. The ρ ₁₅ of the lubricating base oils (II) and (V) is preferably 0.835 g / cm ³ or less, more preferably 0.830 g / cm ³ or less. The ρ ₁₅ of the lubricating base oils (III) and (VI) is preferably 0.840 g / cm ³ or less, more preferably 0.835 g / cm ³ or less.

  In addition, the density in 15 degreeC said by this invention means the density measured in 15 degreeC based on JISK2249-1995.

The aniline point (AP (° C.)) of the lubricating base oil of the present invention depends on the viscosity grade of the lubricating base oil, but is not less than the value of A represented by the following formula (3), that is, AP ≧ A is preferred.
A = 4.1 × kv100 + 97 (3)
[Wherein, kv100 represents the kinematic viscosity (mm ² / s) of the lubricating base oil at 100 ° C. ]

  When AP <A, viscosity-temperature characteristics and thermal / oxidative stability, volatilization prevention properties and low-temperature viscosity characteristics tend to decrease, and when additives are added to the lubricating base oil In addition, the effectiveness of the additive tends to decrease.

  For example, the AP of the lubricating base oils (I) and (IV) is preferably 108 ° C. or higher, more preferably 110 ° C. or higher, and still more preferably 112 ° C. or higher. The AP of the lubricating base oils (II) and (V) is preferably 113 ° C. or higher, more preferably 116 ° C. or higher, still more preferably 118 ° C. or higher, and particularly preferably 120 ° C. or higher. The AP of the lubricating base oils (III) and (VI) is preferably 125 ° C. or higher, more preferably 127 ° C. or higher, and still more preferably 128 ° C. or higher. In addition, the aniline point as used in the field of this invention means the aniline point measured based on JISK2256-1985.

  Further, the NOACK evaporation amount of the lubricating base oil of the present invention is not particularly limited. For example, the NOACK evaporation amount of the lubricating base oils (I) and (IV) is preferably 20% by mass or more, more preferably 25 mass% or more, More preferably, it is 30 or more, Preferably it is 50 mass% or less, More preferably, it is 45 mass% or less, More preferably, it is 42 mass% or less. The NOACK evaporation amount of the lubricating base oils (II) and (V) is preferably 6% by mass or more, more preferably 8% by mass or more, still more preferably 10% by mass or more, and preferably 20%. It is not more than mass%, more preferably not more than 16 mass%, still more preferably not more than 15 mass%, particularly preferably not more than 14 mass%. Further, the NOACK evaporation amount of the lubricating base oils (III) and (VI) is preferably 1% by mass or more, more preferably 2% by mass or more, and preferably 8% by mass or less, more preferably 6%. It is at most 4% by mass, more preferably at most 4% by mass. When the NOACK evaporation amount is the lower limit value, it tends to be difficult to improve the low temperature viscosity characteristics. Further, when the NOACK evaporation amount exceeds the upper limit value, when the lubricating base oil is used as the lubricating oil for an internal combustion engine, the evaporation loss amount of the lubricating oil increases, and accordingly, catalyst poisoning is promoted. Therefore, it is not preferable. In addition, the NOACK evaporation amount as used in the field of this invention means the evaporation loss amount measured based on ASTM D 5800-95.

  The distillation properties of the lubricating base oil of the present invention are preferably gas chromatography distillation, wherein the initial boiling point (IBP) is 290 to 440 ° C. and the end point (FBP) is 430 to 580 ° C. Obtaining the lubricating base oils (I) to (III) and (IV) to (VI) having the preferred viscosity range described above by rectifying one or more fractions selected from a certain fraction Can do.

  For example, regarding the distillation properties of the lubricating base oils (I) and (IV), the initial boiling point (IBP) is preferably 260 to 360 ° C, more preferably 300 to 350 ° C, and still more preferably 310 to 350 ° C. It is. Moreover, 10% distillation temperature (T10) becomes like this. Preferably it is 320-400 degreeC, More preferably, it is 340-390 degreeC, More preferably, it is 350-380 degreeC. The 50% distillation point (T50) is preferably 350 to 430 ° C, more preferably 360 to 410 ° C, and still more preferably 370 to 400 ° C. Moreover, 90% distillation point (T90) becomes like this. Preferably it is 380-460 degreeC, More preferably, it is 390-450 degreeC, More preferably, it is 400-440 degreeC. Moreover, an end point (FBP) becomes like this. Preferably it is 420-520 degreeC, More preferably, it is 430-500 degreeC, More preferably, it is 440-480 degreeC. Moreover, T90-T10 becomes like this. Preferably it is 50-100 degreeC, More preferably, it is 55-85 degreeC, More preferably, it is 60-70 degreeC. Moreover, FBP-IBP becomes like this. Preferably it is 100-250 degreeC, More preferably, it is 110-220 degreeC, More preferably, it is 120-200 degreeC. Moreover, T10-IBP becomes like this. Preferably it is 10-80 degreeC, More preferably, it is 15-60 degreeC, More preferably, it is 20-50 degreeC. Moreover, FBP-T90 becomes like this. Preferably it is 10-80 degreeC, More preferably, it is 15-70 degreeC, More preferably, it is 20-60 degreeC.

  Moreover, regarding the distillation properties of the lubricating base oils (II) and (V), the initial boiling point (IBP) is preferably 300 to 380 ° C, more preferably 320 to 370 ° C, still more preferably 330 to 360 ° C. It is. Moreover, 10% distillation temperature (T10) becomes like this. Preferably it is 340-420 degreeC, More preferably, it is 350-410 degreeC, More preferably, it is 360-400 degreeC. The 50% distillation point (T50) is preferably 380 to 460 ° C, more preferably 390 to 450 ° C, and still more preferably 400 to 460 ° C. Moreover, 90% distillation point (T90) becomes like this. Preferably it is 440-500 degreeC, More preferably, it is 450-490 degreeC, More preferably, it is 460-480 degreeC. Moreover, an end point (FBP) becomes like this. Preferably it is 460-540 degreeC, More preferably, it is 470-530 degreeC, More preferably, it is 480-520 degreeC. Moreover, T90-T10 becomes like this. Preferably it is 50-100 degreeC, More preferably, it is 60-95 degreeC, More preferably, it is 80-90 degreeC. Moreover, FBP-IBP becomes like this. Preferably it is 100-250 degreeC, More preferably, it is 120-180 degreeC, More preferably, it is 130-160 degreeC. Moreover, T10-IBP becomes like this. Preferably it is 10-70 degreeC, More preferably, it is 15-60 degreeC, More preferably, it is 20-50 degreeC. Moreover, FBP-T90 becomes like this. Preferably it is 10-50 degreeC, More preferably, it is 20-40 degreeC, More preferably, it is 25-35 degreeC.

  Further, regarding the distillation properties of the lubricating base oils (III) and (VI), the initial boiling point (IBP) is preferably 320 to 480 ° C, more preferably 350 to 460 ° C, still more preferably 380 to 440 ° C. It is. Moreover, 10% distillation temperature (T10) becomes like this. Preferably it is 420-500 degreeC, More preferably, it is 430-480 degreeC, More preferably, it is 440-460 degreeC. The 50% distillation point (T50) is preferably 440 to 520 ° C, more preferably 450 to 510 ° C, and still more preferably 460 to 490 ° C. Moreover, 90% distillation point (T90) becomes like this. Preferably it is 470-550 degreeC, More preferably, it is 480-540 degreeC, More preferably, it is 490-520 degreeC. Moreover, an end point (FBP) becomes like this. Preferably it is 500-580 degreeC, More preferably, it is 510-570 degreeC, More preferably, it is 520-560 degreeC. Moreover, T90-T10 becomes like this. Preferably it is 50-120 degreeC, More preferably, it is 55-100 degreeC, More preferably, it is 55-90 degreeC. Moreover, FBP-IBP becomes like this. Preferably it is 100-250 degreeC, More preferably, it is 110-220 degreeC, More preferably, it is 115-200 degreeC. Moreover, T10-IBP becomes like this. Preferably it is 10-100 degreeC, More preferably, it is 15-90 degreeC, More preferably, it is 20-50 degreeC. Moreover, FBP-T90 becomes like this. Preferably it is 10-50 degreeC, More preferably, it is 20-40 degreeC, More preferably, it is 25-35 degreeC.

  In each of the lubricating base oils (I) to (VI), IBP, T10, T50, T90, FBP, T90-T10, FBP-IBP, T10-IBP, and FBP-T90 are set to the above preferable ranges. Further, it is possible to further improve the low temperature viscosity and further reduce the evaporation loss. In addition, about each of T90-T10, FBP-IBP, T10-IBP, and FBP-T90, when the distillation range is made too narrow, the yield of lubricating base oil is deteriorated, which is not preferable in terms of economy. .

  In the present invention, IBP, T10, T50, T90 and FBP mean distillate points measured in accordance with ASTM D 2887-97, respectively.

  Moreover, although the residual metal content in the lubricating base oil of the present invention is derived from the metal content contained in the catalyst and raw materials which are inevitably mixed in the production process, it is preferable that the residual metal content is sufficiently removed. For example, the contents of Al, Mo, and Ni are each preferably 1 mass ppm or less. If the content of these metals exceeds the above upper limit, the function of the additive blended with the lubricating base oil tends to be inhibited.

  In addition, the residual metal content as used in the field of this invention means the metal content measured based on JPI-5S-38-2003.

  The lubricating base oil of the present invention having the above-described structure is excellent in viscosity-temperature characteristics and improved in friction characteristics of the lubricating base oil itself, achieving an improvement in friction reduction effect and thus an improvement in energy saving. Is something that can be done. In addition, when an additive is blended in the lubricating base oil of the present invention, the function of the additive (the effect of improving thermal and oxidation stability by an antioxidant, the effect of reducing friction by a friction modifier, the resistance to wear by an anti-wear agent). Abrasion improvement effect, etc.) can be expressed at a higher level. Therefore, the lubricating base oil of the present invention can be suitably used as a base oil for various lubricating oils. Specifically, the lubricating base oil of the present invention is used for internal combustion engines such as gasoline engines for passenger cars, gasoline engines for motorcycles, diesel engines, gas engines, gas heat pump engines, marine engines, and power generation engines. Lubricants (lubricants for internal combustion engines), automatic transmissions, manual transmissions, continuously variable transmissions, final reduction gears, etc., used for drive transmission devices (oils for drive transmission devices), shock absorbers, construction machinery, etc. Hydraulic oil, compressor oil, turbine oil, industrial gear oil, refrigeration oil, rust preventive oil, heat medium oil, gas holder seal oil, bearing oil, paper machine oil, machine tool oil, slip Guide surface oil, electrical insulating oil, cutting oil, press oil, rolling oil, heat treatment oil, etc., and by using the lubricating base oil of the present invention for these applications, the viscosity of each lubricating oil- Degrees characteristic, heat and oxidation stability, energy saving, improvement in properties such as fuel economy, and so the reduction of long life and hazardous substances in the lubricating oil can be achieved at a high level.

  When the lubricating base oil of the present invention is used as the base oil of the lubricating oil, the lubricating base oil of the present invention may be used alone, or the lubricating base oil of the present invention may be one of other base oils or You may use together with 2 or more types. In addition, when using together the lubricating base oil of this invention and other base oils, it is preferable that the ratio of the lubricating base oil of this invention in those mixed base oils is 30 mass% or more, and 50 More preferably, it is more than 70 mass%, and still more preferably 70 mass% or more.

Although it does not restrict | limit especially as another base oil used together with the lubricating base oil of this invention, As mineral base oil, for example, solvent refined mineral oil whose kinematic viscosity in 100 degreeC is 1-100 mm < ² > / s, hydrogenation Cracked mineral oil, hydrorefined mineral oil, solvent dewaxing base oil and the like.

  Synthetic base oils include poly α-olefins or hydrides thereof, isobutene oligomers or hydrides thereof, isoparaffins, alkylbenzenes, alkylnaphthalenes, diesters (ditridecyl glutarate, di-2-ethylhexyl adipate, diisodecyl adipate, ditridec Decyl adipate, di-2-ethylhexyl sebacate, etc.), polyol ester (trimethylolpropane caprylate, trimethylolpropane pelargonate, pentaerythritol 2-ethylhexanoate, pentaerythritol pelargonate, etc.), polyoxyalkylene glycol, dialkyl Examples thereof include diphenyl ether and polyphenyl ether, and among them, poly α-olefin is preferable. As the poly α-olefin, typically, an oligomer or co-oligomer (1-octene oligomer, decene oligomer, ethylene-propylene co-oligomer, etc.) having 2 to 32 carbon atoms, preferably 6 to 16 carbon atoms, and those. Of the hydrides.

  The production method of the poly-α-olefin is not particularly limited. For example, Friedel-Crafts catalyst containing a complex of aluminum trichloride or boron trifluoride with water, alcohol (ethanol, propanol, butanol, etc.), carboxylic acid or ester. And a method of polymerizing α-olefin in the presence of a polymerization catalyst such as

  Moreover, it does not restrict | limit especially as an additive mix | blended with the lubricating base oil of this invention, The arbitrary additives conventionally used in the field | area of a lubricating oil can be mix | blended. Specific examples of such lubricating oil additives include antioxidants, ashless dispersants, metallic detergents, extreme pressure agents, antiwear agents, viscosity index improvers, pour point depressants, friction modifiers, oiliness agents. , Corrosion inhibitors, rust inhibitors, demulsifiers, metal deactivators, seal swelling agents, antifoaming agents, colorants and the like. These additives may be used individually by 1 type, and may be used in combination of 2 or more type.

  EXAMPLES Hereinafter, although this invention is demonstrated more concretely based on an Example and a comparative example, this invention is not limited to a following example at all.

[Example 1, Comparative Example 1]
The fraction separated by vacuum distillation in the step of refining the solvent refined base oil was subjected to hydrogenation after solvent extraction with furfural and then dewaxed with a methyl ethyl ketone-toluene mixed solvent. A wax obtained by further deoiling the slack wax removed during the solvent dewaxing (hereinafter referred to as “WAX1”) was used as a raw material for the lubricating base oil. Table 1 shows the properties of WAX1.

Next, hydrocracking of WAX1 was performed under the conditions of a hydrogen partial pressure of 5 MPa, an average reaction temperature of 350 ° C., and LHSV1hr ⁻¹ in the presence of a hydrocracking catalyst. As the hydrocracking catalyst, a catalyst in which 3% by mass of nickel and 15% by mass of molybdenum were supported on an amorphous silica / alumina carrier (silica: alumina = 20: 80 (mass ratio)) was used in a sulfurized state.

  Next, the cracked product obtained by the above hydrocracking was distilled under reduced pressure to obtain a 26% by volume lubricating oil fraction with respect to the raw material oil. For this lubricating oil fraction, solvent dewaxing was performed using a methyl ethyl ketone-toluene mixed solvent at a solvent / oil ratio of 4 times and a filtration temperature of -25 ° C., and light and heavy components were separated by distillation. A lubricating base oil having the composition and properties shown in Table 2 was obtained. In Table 2, as Comparative Example 1, the composition and properties of a conventional lubricating base oil obtained using WAX 1 are also shown. In Table 1, “the ratio of the components derived from normal paraffin in the urea adduct” is obtained by performing a gas chromatography analysis on the urea adduct obtained in the measurement of the urea adduct value. Yes (the same applies hereinafter).

[Example 2, Comparative Example 2]
In Example 2, a wax obtained by further deoiling WAX1 (hereinafter referred to as “WAX2”) was used as a raw material for the lubricant base oil. Table 3 shows the properties of WAX2.

  Next, hydrocracking / hydroisomerization, solvent dewaxing, and distillation were carried out in the same manner as in Example 1 except that WAX2 was used instead of WAX1, and a lubricant having the composition and properties shown in Table 4 was obtained. An oil base oil was obtained. In Table 4, as Comparative Example 2, the composition and properties of a conventional lubricating base oil obtained using WAX 2 are also shown.

[Example 3, Comparative Example 3]
In Example 3, an FT wax having a paraffin content of 95% by mass and having a carbon number distribution of 20 to 80 (hereinafter referred to as “WAX3”) was used. Table 5 shows the properties of WAX3.

  Next, hydrocracking / hydroisomerization, solvent dewaxing, and distillation were performed in the same manner as in Example 1 except that WAX3 was used instead of WAX1, and a lubricating oil having the composition and properties shown in Table 6 was obtained. A base oil was obtained. In Table 6, as Comparative Example 3, the composition and properties of a conventional lubricating base oil obtained using WAX3 are also shown.

Claims (4)

  It is obtained from a raw material oil containing normal paraffin, has a urea adduct value of 7% by mass or less, a viscosity index of 100 or more, and a saturated content of 90% by mass based on the total amount of the lubricating base oil. % Lubricating base oil characterized by being at least%. NH ₃ to the carrier desorption of the fraction of the NH ₃ is 80% or less at 300 to 800 ° C. relative to the total desorption of NH ₃ in the desorption temperature dependence evaluation, at least one of the periodic table Group VIa metals And a first step of preparing a hydrocracking catalyst on which at least one of the Group VIII metals is supported,
In the presence of the hydrocracking catalyst, a feed oil containing 50% by volume or more of slack wax, hydrogen partial pressure of 0.1-14 MPa, average reaction temperature of 230-430 ° C., LHSV 0.3-3.0 hr ⁻¹ , hydrogen oil A second step of hydrocracking at a ratio of 50-14000 scf / b;
A third step of distilling and separating the cracked product oil obtained in the second step to obtain a lubricating oil fraction;
The lubricating oil fraction obtained in the third step is dewaxed, the urea adduct value is 7% by mass or less, the viscosity index is 100 or more, and the content of the saturated component is a lubricating oil base oil. A fourth step of obtaining a lubricating base oil that is 90% by mass or more based on the total amount;
A method for producing a lubricating base oil, comprising: A fifth step of hydrocracking a feedstock containing paraffinic hydrocarbons in the presence of a catalyst;
Dewaxing the product obtained in the fifth step or the lubricating oil fraction recovered from the product by distillation separation, the urea adduct value is 7% by mass or less, the viscosity index is 100 or more, and A sixth step of obtaining a lubricating base oil having a saturated content of 90% by mass or more based on the total amount of the lubricating base oil;
A method for producing a lubricating base oil, comprising: A lubricating oil composition comprising the lubricating base oil according to claim 1.