KR101654412B1 - Method for preparing single grade lube base oil - Google Patents

Abstract

(A) providing a mixture of VR / AR and VR / AR to a solvent deasphalted (SDA) apparatus to obtain asphalt-free deasphalted oil (DAO) ; (b) subjecting the deasphalted oil (DAO) to hydrogenation (HDT) in the presence of a hydrogenation catalyst; (c) introducing the HDT oil fraction into the separation unit Fs to obtain a hard stream and a heavy stream; And (d) mixing the light and heavy streams to produce a single grade lubricant oil comprising the main product main product stage. The method of producing a single-grade lubricating oil according to the present invention in a large amount can remarkably increase the production amount of the lubricating oil by eliminating the constraint of the raw material property.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a method for preparing a single-

The present invention relates to a method for mass production of a single grade lubricating oil.

Viscosity is an important property of fluidity. It refers to the internal resistance when fluid is to be moved. It is also called dynamic viscosity or absolute viscosity. The kinematic viscosity is determined by dividing the absolute viscosity by the density of the fluid. In general, kinematic viscosity refers to the kinematic viscosity of a lubricant. When selecting the viscosity of the lubricating oil, the viscosity should be selected in consideration of the characteristics of the equipment. However, if the viscosity of the lubricating oil is too high, the internal resistance to the fluid flow becomes large, which causes an increase in power consumption, If the lubricating oil having an excessively low viscosity is used, various problems arise due to oil film breakage.

The viscosity of the lubricating oil decreases as the temperature rises and increases as the temperature drops. This is the natural physical characteristic of the lubricating oil. The viscosity index is a numerical value of the change in viscosity with such temperature change. It is calculated by comparing the viscosity index of a specific oil with the viscosity index of petroleum Pennsylvania which is rich in paraffinic system as 100 and the viscosity index of crude oil of Gulf Coast with a lot of naphthenic system as zero. The viscosity index is a relative change in the viscosity change with respect to the temperature change. The higher the viscosity index, the less the viscosity changes with respect to the temperature change. If the viscosity index is high, the viscosity change with temperature is small, so it is good to obtain the expected lubrication effect even if the temperature changes.

In general, excellent lubricating oils have a high viscosity index, excellent stability (oxidation, heat, ultraviolet ray, etc.) and low volatility. The American Petroleum Institute (API) classifies lube oils according to quality as Table 1 below.

 Classification  Sulfur (%)  Saturation (%)  Viscosity Index (VI) Group I  > 0.03  <90  80-120 Group II  0.03  ≥ 90  80-120 Group III  0.03  ≥ 90  120 or more Group Ⅳ (Group Ⅳ)  All PolyAlphaOlefins (PAO)

Generally, the lubricating oil produced by the solvent extraction method of the mineral oil-based lubricant oil is mainly group I, the lubricating oil produced by the hydrogenation reforming method is mainly the group II, and the lubricating oil having high viscosity index produced by the high- III.

On the other hand, when classifying the lubricant oil by the viscosity grade, it is possible to distinguish between a neutral (N) lubricant oil and a bright stock (BS) lubricant oil passage. In the neutral lubricant oil, Brightstock is a very viscous oil coming from the bottom of the tower when distilled under reduced pressure.

In general, the general manufacturing method of the Group II lubricant oil used for general purpose is a process of making a raw material, a process of removing impurities of a raw material through a hydrogenation reforming (HDT) process and improving a property, and finally, a wax for improving fluidity. Removal process.

The lubricant oil is graded according to the kinematic viscosity, and most of them produce the raw material according to the product grade in the raw material manufacturing process. Especially, in the base oil plant, which requires production of various grades, the raw material is manufactured by using the solvent deasphaling (SDA) process, which is a decompression distillation column (VDU) and solvent extraction process, And fine control of the properties of the raw materials is performed by blending through a large-scale tank facility at the rear end. In addition, the company has a tank facility for blending the waxy oil produced at the end of the hydrotreating (HDT) process for additional property management and product grade diversification. Production of various grades has flexibility in overall quality control due to various property management methods, but it has various operation modes and requires a lot of tank facilities. In order to satisfy the kinematic viscosity and viscosity index, which are the most important specifications of lubricant oil, raw materials are first processed to satisfy viscosity index in hydrotreating (HDT) process by controlling distillation and kinematic viscosity of raw materials. Check if there is a problem and adjust the kinematic viscosity of the raw material when a problem arises. Depending on the oil refining company, the HDT process may be completed at the end of the hydrotreating (HDT) process to store the hydrotreated raw material in the tank, and then blend the oil from each tank to solve the problem of controlling the kinematic viscosity .

That is, in general lube oil manufacturing equipments, in order to simultaneously satisfy the kinematic viscosity and viscosity index of the target lubricant oil grade, it is necessary to manage the properties of raw materials injected into the hydrogenation reforming (HDT) process, In order to blend the semi-finished products of the grade, a large-scale tank is installed at the end of each process, and a lot of cost is taken to derive a proper operation plan.

Disclosure of Invention Technical Problem [8] Accordingly, the present invention has been made in order to solve the above-mentioned problems, and it is an object of the present invention to provide a method for controlling a viscosity index in a hydrogenation reforming (HDT) And to provide a method for manufacturing a single grade lubricating oil in large quantities.

In one aspect, a method of mass-producing a single grade lubricant oil is provided. The method comprises the steps of: (a) feeding a mixture (VR / AR) of a reduced pressure residual oil (VR) and an atmospheric pressure residual oil (AR) to a solvent deasphalting device to obtain asphalt-free deasphalted oil; (b) hydrogenating the deasphalted oil in the presence of a hydrogenation catalyst to adjust the viscosity index; (c) introducing the hydrogen-modified oil into the separator in the step (b) to obtain a hard stream and a heavy stream; And (d) mixing the hard stream and the heavy stream to obtain a master product with controlled kinematic viscosity.

According to one embodiment, the method further comprises dewaxing the main product after step (d).

According to another embodiment, when the kinetic viscosity of the main product is out of specification, a portion of the hard stream or a portion of the heavy stream is sloped.

According to another embodiment, the HDT oil fraction in step (b) has a viscosity index (VI) of 112 to 120.

According to another embodiment, the main product obtained by the step (d) has a kinematic viscosity of 10.8 to 11.2 cSt at 100 ° C.

According to still another embodiment, the deasphalted oil (DAO) introduced into the step (b) has an unlimited dynamic viscosity specification.

According to another embodiment, the solvent deasphalted (SDA) of step (a) is subjected to a reaction temperature of 55 to 70 ° C, a reaction pressure of 45 to 47 kg / cm 2 g, and a reaction pressure of 1.0 to 2.6 hr ^-1 Of space velocity (LHSV).

According to another embodiment, the hydrotreating (HDT) of step (b) is carried out at a reaction temperature of 360 to 410 ° C, a reaction pressure of 160 to 180 kg / cm 2 g and a space velocity (LHSV) of 0.25 to 0.5 hr ^-1 . Lt; / RTI &gt;

According to yet another embodiment, the hard and hard streams in step (d) are mixed without a mixing vessel to form a master product.

According to another embodiment, the dewaxed master product has a viscosity index of 100 to 108 and a kinematic viscosity at 100 DEG C of 11.4 to 11.8 cSt.

According to another embodiment, the mixture of step (a) is a mixture of normal pressure residual solvent and reduced pressure residual oil in a ratio of 1: 1.

The method of manufacturing a single-grade lubricating oil according to the embodiment of the present invention can dramatically increase the production amount of the lubricating oil by eliminating the constraint of the raw material property.

1 is a block diagram illustrating a method for manufacturing a single grade lubricant oil according to one embodiment of the present invention;
2 is a schematic view of a separator according to one embodiment of the present invention.

BRIEF DESCRIPTION OF THE DRAWINGS The objectives, specific advantages and novel features of the present invention will become more apparent from the following detailed description taken in conjunction with the accompanying drawings, in which: FIG. In the following description, well-known functions or constructions are not described in detail since they would obscure the invention in unnecessary detail.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.

1 is a block diagram illustrating a method of manufacturing a single grade lubricant oil according to one embodiment of the present invention.

Referring to FIG. 1, a method of manufacturing a single-grade lubricant oil according to an embodiment of the present invention includes the steps of (a) mixing a mixture (VR / AR) of a reduced pressure residual oil (VR) To obtain an asphalt-free deasphalted oil; (b) hydrogenating the deasphalted oil in the presence of a hydrogenation catalyst to adjust the viscosity index; (c) introducing the hydrogen-modified oil into the separator in the step (b) to obtain a hard stream and a heavy stream; And (d) mixing the hard stream and the heavy stream to obtain a master product with controlled kinematic viscosity.

Hereinafter, each process according to the present invention will be described in detail.

(1) raw material manufacturing process

The hydrocarbon used as the feedstock in the deasphalted (SDA) apparatus of the present invention has a boiling point equal to or higher than that of gasoline such as a mixture (AR / VR) of atmospheric residual oil and reduced pressure residual oil, Material. The reduced-pressure residual oil can be obtained by directly obtaining the crude oil through a vacuum distillation process or by distilling the atmospheric residual oil separated from the atmospheric distillation column under reduced pressure.

The hydrocarbon feedstock is fed to a solvent deasphalted (SDA) process to remove asphalt and impurities. The solvent deasphalted (SDA) process according to one embodiment of the present invention is carried out at a reaction temperature of 55 to 70 占 폚, a reaction pressure of 45 to 47 kg / cm2g, and a space velocity (LHSV) of 1.0 to 2.6 ^hr & do.

When the reaction temperature is lower than 55 ℃ based on the solvent propane (C3), it is difficult to separate the DAO from the pitch, and the DAO yield is lower than 70 ℃, and the pitch is too thin, so it is used as asphalt product. it's difficult.

When the reaction pressure is below 45kg / ㎠g, it is difficult to maintain the supercritical separation condition in the separation drum between the post - stage DAO and the solvent. At 47kg / ㎠g, it approaches the mechanical design limit of the apparatus.

If the space velocity is less than 1.0hr ^{- 1} , there is no problem in the extraction operation. However, the operation is less than the minimum operation point of other equipments in the applicable process and it is difficult to operate the extraction tower in case of more than 2.6hr ^{- 1} .

As the solvent used in the solvent deasphalting (SDA) process, a normal or isoparaffinic solvent having 3 to 6 carbon atoms is mainly used. More specifically, normal propane, n-butane, isobutane, n-pentane, &Lt; / RTI &gt; In addition, the yield of deasphalted oil (DAO) versus mixture (VR / AR) of decompression residue and atmospheric residue with raw materials tends to increase as the number of carbon atoms of solvent varies depending on operating conditions and solvent, To 80%.

Deasphalted oil (DAO) produced through this solvent deasphalting process (SDA) contains metal and residual carbon (CCR) content, but high aromatics ratio and high distillation point oil content.

On the other hand, in a lube oil production plant requiring various grades, a vacuum distillation column (VDU) and a solvent deasphalted (SDA) apparatus are used to produce tailor-made raw materials. Dea asphalt oil (DAO) (MVGO) and HVGO (Heavy Vacuum Gas Oil), which are produced from the MVGO, and blend the raw materials supplied from these tanks to control the properties of the raw materials. .

However, in the present invention, in order to concentrate on a single-grade mass production, only the SDA process is adopted as the raw material manufacturing process, and a large-scale blending facility (tank) for controlling the property of the separate VDU and the lubricant oil product is omitted, Simplified investment. In the embodiment of the present invention, since there is no VDU facility, the AR and VR are simultaneously supplied to the SDA and the DAO is controlled by controlling the operating parameters to produce the DAO tailored to the target lube oil product. However, there is no control variable for satisfying both the kinematic viscosity and the viscosity index of the final product because there are no raw / semi-product mixing tanks in the existing multi-grade lubricant oil production process, This is solved by controlling the constellation in the separation unit described later.

(2) Hydrotreating (HDT) process

The DAO removes impurities such as sulfur, nitrogen, metal, and polycyclic aromatic hydrocarbons (PCA) contained in DAO through a hydrogenation process (HDT) in the presence of a hydrogenation catalyst, The aromatic component contained in the hydrogen saturation reaction is converted into a lead-based component or the like. The objective of hydrotreating (HDT) is to remove impurities that can make the ratio of paraffin, pewter, and aromatics compatible with the quality and composition of the lubricant oil, and to be a high quality lubricant oil. Especially, it is the main purpose to remove the impurities which can act as a catalyst poison in the downstream dewaxing (or isomerization) process and the hydrogenation finishing (HDF) process catalyst below the target value.

The hydrogenation reforming process (HDT) is carried out at a reaction temperature of 300-410 ° C., a reaction pressure of 160-180 kg / cm 2 g, a space velocity of 0.25-0.5 hr ^-1 (LHSV) and a feedstock of 850-1,250 Nm 3 / (For example, sulfur, nitrogen, metal, etc.) contained in the feedstock and an aromatic compound of 2 or more rings in an optimum reaction temperature, reaction pressure, and hydrogen supply conditions, Can be dramatically reduced. At this time, it is important to drive the hydrogenation treatment with a degree of severity within a range satisfying the impurity target value which does not affect the lifetime of the catalyst in the rear end. The reason for this is that as the degree of severity increases, the viscosity decrease width of the reactant after the reaction becomes larger, resulting in a loss in the yield rate of the lubricant oil.

The catalyst used in the hydrotreating (HDT) process is preferably one or more selected from Group 6, Group 9 to Group 10 metals of the periodic table, more preferably selected from Co-Mo, Ni-Mo, More than one is selected. However, the hydrogenation catalyst used in the present invention is not limited thereto, and any type of hydrogenation catalyst may be used as long as it is a hydrogenation catalyst having an effect of hydrogen saturation reaction and removal of impurities.

Oil fractions which have undergone the hydrogenation reforming (HDT) reaction are remarkably reduced in impurities and have an appropriate aromatic content. Generally, the sulfur content (preferably 100 ppm or less) of not more than 150 ppm and not more than 50 ppm (Preferably 10 ppm or less) of nitrogen.

Since the oil after the hydrotreating (HDT) process contains very low impurities, the catalytic dewaxing reaction (CDW) at the downstream stage is more stably and actively performed. As a result, the yield in the production of the lubricating oil is high Is low), it is possible to produce a high-quality lubricating oil with excellent selectivity.

(3) Separation process

2 is a schematic diagram of a fractionation section (Fs) according to one embodiment of the present invention.

The separator is a device for separating the reactants having undergone the high-pressure hydrogenation (HDT) process into a plurality of streams. As shown in FIG. 2, the hydrogenation reforming (HDT) reactant is separated at the separator into a diesel (DSL) stream, a low-grade hard lube oil stream, a light stream, and a heavy stream. When the main product is produced by blending the hard product and the heavy product and the kinetic viscosity of the main product is high, the kinetic viscosity of the main product can be freely controlled by sloping a part of the heavy stream. Slop means oil that can not be used as a main product and is generally discarded. It is usually re-used as a raw material of the process or reused as a raw material of another process.

On the other hand, if the kinetic viscosity of the main product is low, the flow of the heavy stream may be increased or a part of the hard stream may be discharged (not shown).

The operation plan for the separation section of the hydrogenation reforming (HDT) process commonly used in the lubricant oil production industry is that the most important kinematic viscosity and viscosity index of the lubricant oil phase are determined in the raw material manufacturing process and the hydrogenation reforming (HDT) process , And only the lower-level light oil is separated from the separation unit at the downstream end. In this operation plan, the viscosity index of the lubricant oil phase falls within the specification, but if the kinematic viscosity is high, the product can not be a normal product and is off-spec product, and there is no way to control the property in the separator. In this case, it is possible to lower the kinematic viscosity by mixing the low-grade hard lubricant oil, which is the upper product, optionally, but it is not possible to meet the volatility standard which is another standard of the lubricant oil.

However, one embodiment of the present invention is a method in which the main product is divided into a hard stream and a heavy stream in the separating unit Fs and blended at the rear end of the separating unit. According to this method, only the viscosity index can be produced in the reaction part of the hydrogenation reforming (HDT) by adjusting the degree of reaction, and the kinematic viscosity of the main product can be freely controlled in the separation part. Therefore, in the hydrotreating (HDT) reaction, it is possible to reduce the burden of adjusting both the kinematic viscosity and the viscosity index, which are the main specifications of the lubricant oil, and to control the dynamic viscosity of the main product.

Thus, it is a major advantage of the present invention that the kinematic viscosity of the product can be adjusted freely regardless of the nature of the raw material. Therefore, the constraint on the shape of the crude oil is completely solved, and the production amount restriction of the raw material production process is eliminated, so that the raw material production amount can be remarkably increased. In addition, the direct connection operation of the SDA-HDT-CDW process for single-grade mass production has become technically feasible.

(4) De-waxing process

The oil fraction discharged from the separation section through the hydrogenation reforming (HDT) reaction is remarkably reduced in impurities and the aromatic content is appropriately adjusted. Usually, considering the effect on the post-stage catalyst, the oil content of not more than 150 ppm (preferably 100 ppm Or less) and a nitrogen content (preferably 10 ppm or less) of 50 ppm or less.

Since the oil after the hydrotreating (HDT) process contains very low impurities, the catalytic dewaxing reaction (CDW) at the downstream stage is more stably and actively performed. As a result, the yield in the production of the lubricating oil is high Is low), it is possible to produce a high-quality lubricating oil with excellent selectivity.

The hydrogenated modified (HDT) oil fraction can be dewaxed in the presence of a dewaxing catalyst. The catalyst dewaxing process according to the present invention means a reaction process for reducing or eliminating N-paraffin which deteriorates low-temperature properties by isomerization reaction or cracking reaction. Therefore, when the catalyst is subjected to the dewaxing reaction, it can have excellent low-temperature properties, so that the specification of the flow point of the lubricant can be met.

The catalytic dewaxing process is carried out at a reaction temperature of 250 to 410 ° C., a reaction pressure of 30 to 200 kg / cm 2 g, a space velocity (LHSV) of 0.1 to 3.0 hr ^-1 and a volume ratio of hydrogen to feedstocks of 150 to 1000 Nm 3 / Lt; / RTI &gt;

The catalyst used in the catalytic dewaxing process includes the carrier and the metal supported thereon. The carrier is a carrier having an acid site selected from molecular sieves, alumina and silica-alumina. The molecular sieve refers to crystalline aluminosilicate (zeolite), SAPO, ALPO and the like, SAPO-11, SAPO-41, ZSM-11, ZSM-22, ZSM-23, ZSM-35 and ZSM-48 as intermediate porous molecular sieves having an oxygen ring (10- Large pore molecular sieves with 12-membered oxygen rings include FAU, Beta and MOR.

The metal used for the dewaxing catalyst includes a metal having a hydrogenating function selected from Group 2, Group 6, Group 8, or Group 9 and Group 10 metals of the periodic table. In particular, Co, Ni, Pt, and Pd are preferred among the Group 9 and Group 10 (i.e., Group III) metals, and Mo and W are preferred among the Group 6 (i.e., Group VIB) metals.

In the case of deasphalted oil (DAO) used as feedstock for catalytic dewaxing processes, the paraffin content is relatively high because it is produced from the extraction top of a solvent asphalt (SDA) process. Therefore, a Ni (Co) / Mo (W) catalyst having a strong cracking function can be used. However, when the catalyst is used, it is preferable to use an isomerization catalyst (Group 10 metal base) which can slightly decrease the yield and lower the viscosity, thereby isomerizing N-paraffin into iso-paraffin to improve the pour point.

(5) Hydrogenated finishing (HTF) process

The dewaxed oil fraction is hydrogenated (HTF) in the presence of a hydrogenation finishing catalyst. Hydrofinishing (HTF) process removes olefins and polycyclic aromatics from dewaxed oils in the presence of hydrogenated finishing catalysts to ensure stability. Particularly in terms of production of lead-based lubricants, Gas hygroscopicity and the like. Is generally carried out under the conditions of a temperature of 150 to 300 ° C, a pressure of 30 to 200 kg / cm 2, a space velocity of 0.1 to 3 h -1 (LHSV) and a volume ratio of hydrogen to the incoming oil of 300 to 1500 Nm 3 / m 3 .

The catalyst used in the hydrogenation finishing step is used by supporting a metal on a carrier, and the metal includes at least one metal selected from Group 6, Group 8, Group 9, Group 10, and Group 11 elements having a hydrogenating function, Ni-Mo, Co-Mo, Ni-W, or precious metals such as Pt and Pd.

As a carrier for the catalyst used in the hydrogenation finishing step, silica, alumina, silica-alumina, titania, zirconia or zeolite having a large surface area can be used, and alumina or silica-alumina is preferably used. The carrier serves to improve the hydrogenation performance by increasing the degree of dispersion of the metal, and it is very important to control the acid point in order to prevent cracking and coking of the product. The effluent that has undergone the hydrotreating (HDT), catalytic de-waxing (CDW) and hydrofinishing (HDF) reaction stages can be used directly as a heavy lubricant flow path.

Hereinafter, the present invention will be described in more detail with reference to the following examples, but the scope of the present invention is not limited thereto.

Example  One

After mixing the atmospheric residue (AR) and the reduced residual oil at a ratio of about 1: 1, the asphalt and impurities are appropriately removed by supplying it to a solder asphalt unit (SDA). (N-C3) was used as a deasphalting solvent, and a deasphalting process was carried out at a reaction temperature of about 55 ° C., a reaction pressure of about 46 kg / cm 2 g, and a space velocity (LHSV) of about 2.6 hr ^-1 (DAO) was prepared. Since it is possible to control the properties of the oil in the HDT rear end separation part, the dynamic viscosity specification of the DAO is not limited. In order to produce the maximum amount of deasphalted oil (DAO) Lt; RTI ID = 0.0 &gt; 55 C. &lt; / RTI & (DAO) in a hydrotreating (HDT) process under a commercial catalyst with HDS (hydrodesulfurization), HDN (hydrogenation denitration) and HDM (hydrosoluble metal) functions at a space velocity (LHSV) of about 0.33 ^hr & The reaction pressure was about 160 kg / cm 2 g, the reaction temperature was about 370 ° C, and the hydrogen and oil ratio were about 1200 NL / L to reduce sulfur to about 10 ppm and nitrogen to about 3 ppm or less. The oil obtained after hydrotreating (HDT) was separated into a heavy stream and a hard stream in a separator, discharged and mixed again to prepare a main product. The main product was treated with pt / zeolite as an isomerization catalyst in a catalytic dewaxing (CDW) step and (pt / pd) / Al2O3 catalyst in a hydrogenation finish (HDF) step. In each step, the reaction pressure was about 170 kg / cm 2 g, the space velocity (LHSV) was about 2.0 hr ^-1 , and the ratio of hydrogen to oil was about 500 Nm 3 / m 3. The reaction temperature was operated at about 325 ° C for the catalytic dewaxing (CDW) process and at about 230 ° C for the hydrofinishing (HTF) process. During the operation, the reaction temperature was controlled so that the pour point of the catalyst dewaxing reaction effluent was below -30 ° C. Table 2 shows the yields of intermediate product and final lubricating oil according to the step 1 according to Example 1.

Comparative Example  One

In Comparative Example 1, the operation of the HDT separator is in a state in which there is no configuration for controlling the oil phase, and the kinematic viscosity of the deasphalted oil (DAO) should be managed in consideration of the characteristics of the final base oil fraction from the solder asphalt unit (SDA) . The kinematic viscosity of deasphalted oil (DAO) was about 15.5 cSt (100 ℃), which was able to satisfy the characteristics of the base oil product stably without special oil phase control in the HDT separation part. The reaction temperature of about 65 ℃, about 46kg / ㎠ g, and a space velocity (LHSV) of about 1.9 ^hr &lt; -1 &gt; to produce a deasphalted oil (DAO). (DAO) in a hydrotreating (HDT) process under a commercial catalyst having HDS (hydrodesulfurization), HDN (hydrogenation denitration) and HDM (hydrosoluble metal) functions at a space velocity (LHSV) of about 0.20 ^{hr "} A reaction pressure of about 160 kg / cm 2, a reaction temperature of about 360 ° C, and a hydrogen and oil ratio of about 1200 NL / L to reduce sulfur to about 10 ppm or less and nitrogen to about 3 ppm or less. The oil obtained after hydrotreating (HDT) was not produced separately from the heavy stream and the light stream in the separation section, but the main product was directly produced only under the separation section. Catalyst dewaxing (CDW) and hydrogenation finish (HTF) after storage in the intermediate semi-finished product tank were carried out under the same conditions as in the examples. Table 2 shows the yields of intermediate products and final lubricating oil according to Comparative Example 1.

fair Example 1 Comparative Example 1 SDA (deasphalting process)
Processing 250000 BPD of raw materials Process raw material 18,000 BPD Production of DAO 10,000 BPD DAO 5,800 BPD production No DAO kinematic viscosity specification DAO Kinematic viscosity standard 15.5 cSt (100 ℃) HDT (hydrogenation reforming process) Production of 6,500 BPD 4,100 BPD production Dewaxing process 5,800 BPD production 3,700 BPD production

As shown in Table 2, according to Example 1, the production constraint of the process of producing deasphalted oil (DAO) by adjusting kinematic viscosity in the deasphalting process (SDA) was completely eliminated, Increased by more than 50%.

AR: atmospheric residue VR: decompressed residue
AR / VR: Atmospheric residuum and decompression residue mixture SDA: Deasphalted
HDT: Hydrogen reforming process Fs: Separation (division) process
De-Waxing: De-waxing process CDW: Catalyst de-waxing process
HDF: Hydrogen Finishing Process FCC: Fluidized Bed Catalytic Reaction Process
DSL: Diesel Heavy Slop: Heavy slop
DAO: Deasphalted oil

Claims (11)

(a) supplying a mixture (VR / AR) of a reduced pressure residual oil (VR) and an atmospheric pressure residual oil (AR) to a solvent deasphalting device to obtain an asphalt-free deasphalted oil;
(b) hydrogenating the deasphalted oil in the presence of a hydrogenation catalyst to adjust the viscosity index;
(c) introducing the hydrogen-modified oil into the separator in the step (b) to obtain a hard stream and a heavy stream; And
(d) mixing said hard stream and said heavy stream to obtain a master product with controlled kinematic viscosity,
Wherein the deasphalted oil introduced into the step (b) has a property free of kinetic viscosity specification. The method according to claim 1,
(e) dewaxing the main product after step (d). The method according to claim 1,
And sloping a portion of the hard stream or a portion of the heavy stream if the kinetic viscosity of the master product is out of specification. The method according to claim 1,
Wherein the hydrogenated oil fraction in the step (b) has a viscosity index of 112 to 120. [ The method according to claim 1,
Wherein the main product obtained in step (d) has a kinematic viscosity of 10.8 to 11.2 cSt at 100 占 폚. delete The method according to claim 1,
The solvent deasphalted in step (a) is carried out at a reaction temperature of 55 to 70 ° C, a reaction pressure of 45 to 47 kg / cm 2 g, and a space velocity (LHSV) of 1.0 to 2.6 hr ^-1 based on the propane solvent By weight based on the weight of the lubricant. The method according to claim 1,
Wherein the hydrogenation of step (b) is carried out at a reaction temperature of 360 to 410 ° C., a reaction pressure of 160 to 180 kg / cm 2 g, and a space velocity (LHSV) of 0.25 to 0.5 hr ^-1 . Gt; The method according to claim 1,
Wherein the hard stream and the heavy stream in step (d) are mixed without a mixing vessel to form a main product. The method of claim 2,
Wherein the dewaxed main product has a viscosity index of 100 to 108 and a kinematic viscosity at 100 DEG C of 11.4 to 11.8 cSt. The method according to claim 1,
Wherein the mixture of step (a) is a mixture of an atmospheric residue oil and a vacuum residue oil at a volume ratio of 1: 1.

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