KR20000003150A - Process for preparing high-level lubricant base oil by binding hydrocracking, catalytic dewaxing and hydrofinishing process in one loop - Google Patents

Abstract

PURPOSE: A process for combining a hydrocracking process and a lubricant base oil process(catalytic dewaxing and hydrofinishing) is provided to produce low pour point fuel oil and high viscosity index lubricant base oil at the same time and control the production rate flexibly according to the market circumstances. CONSTITUTION: A conventional manufacturing method of lubricant base oil is as follows. Atmospheric residue(AR) is distilled under reduced pressure at a vacuum tower(VT1) to give vacuum gas oil(VGO), which is hydrotreated at a hydrotreating reactor(R1), hydrocracked at a hydrocracking reactor(R2), distilled with light distillate from a stripper(ST) at an atmospheric tower(AT) to separate fuel and hydrocrackate. Remaining hydrocrackate is hydrocracked at the 2nd step hydrocracking reactor(R3), dewaxed catalytically, hydrofinished, and sent to the stripper(ST). Light distillate is sent to the atmospheric tower(AT), remaining lubricant base oil is sent to a vacuum tower(VT2) to produce lubricant base oil. The new 3rd step hydrocracking reactor(R4) is constructed following behind the 2nd step hydrocracking reactor(R3) to perform a catalytic dewaxing and a hydrofinishing continuously in one reactor and an amine absorption tower is constructed to control the concentration of hydrogen sulfide.

Description

Combined hydrocracking, catalyst dewaxing, and hydrostable stabilization in one loop

The present invention relates to a process that enables the simultaneous production of fuel oil with low pour point and lubricating base oil with high viscosity index by combining two-stage hydrolysis process and lubricating base oil process (catalyst dewaxing and hydrogenation stabilization process). Or it is to adjust the lube base oil production rate elastically.

이론) Theoretical background of hydrocracking process and lube base oil process

The hydrocracking process may focus on fuel oil production by varying the fuel oil conversion rate depending on the purpose, and may also focus on the production of lubricating base oil raw materials.

For convenience, the hydrocracking process mainly for fuel oil production is referred to as the fuel hydrocracking process, and the hydrocracking process mainly for the production of lubricant base oil is classified as a lubricant hydrocracking process.

The fuel oil hydrocracking process and the lubricating oil hydrocracking process have been developed independently of each other. For fuel oil production, the fuel oil conversion rate of the reduced pressure gas oil is mainly 50 to 90% (over 90% of the total fuel oil conversion rate). In order to produce lubricating base oil (hydrolysis cracking residue oil), the fuel oil conversion rate per pressure of the reduced-pressure gas oil is mainly 20 to 30%. Of course, the fuel oil conversion per pass of the vacuum gas oil can also be 30 to 50%.

In the fuel oil hydrocracking process, decompression gas oil is decomposed and converted to light oil, especially kerosene or diesel, and various hydrocracking catalysts have been developed and used to increase the decomposition conversion rate while treating a large amount of vacuum gas oil. Is mainly an amorphous silica-alumina catalyst supported on nickel-molybdenum and the like.

On the other hand, in the lubricating oil hydrocracking process, the aromatic compounds present in the reduced-pressure gas oil are decomposed and saturated at the same time to be converted into lead-sensing compounds. The catalyst used here is mainly amorphous alumina or amorphous silica-alumina supported with nickel-tungsten or the like. Catalyst and the like. Here some sulfur and some nitrogen are removed by conversion to hydrogen sulfide and ammonia.

When only fuel oil is produced, the hydrocracking process may exist as a single process, but when producing lube base oil, a dewaxing process and a hydrostable stabilization process are required along with the hydrocracking process. That is, lubricating base oil requires conditions such as proper boiling point and viscosity, high viscosity index, low pour point, excellent color and stability. A stabilization process is required.

The hydrocracked residue oil, which is converted to light oil in the hydrocracking process, can be used as a raw material for lubricating base oil. The lubricating base oil has a suitable boiling point, viscosity and high viscosity index, but has a high pour point and poor color and stability. It goes through the catalytic dewaxing process for the drop and the hydrogenation stabilization process to improve the color and stability.

In the catalyst stripping process, a zeolite catalyst such as ZSM-5 is used to selectively decompose only lead components, thereby lowering the pour point, and in the hydrostable stabilization process, olefins formed by side reactions during catalyst stripping and unreacted in the previous hydrocracking process. The residual sulfur, nitrogen and polynuclear aromatic compounds are hydrogenated in the presence of a nickel-tungsten-supported alumina catalyst to saturate the olefin and polynuclear aromatic compounds and release sulfur or nitrogen as hydrogen sulfide or ammonia to improve the color and stability of the lubricant base oil.

In the fuel oil hydrocracking process, an amorphous silica-alumina catalyst supported with nickel-molybdenum and the like was conventionally used. However, due to poor activity in increasing the conversion rate, the fuel oil conversion rate was increased by replacing the Y-zeolite catalyst with nickel-molybdenum and the like. (Hereinafter the “fuel oil conversion rate” is referred to as the “conversion rate”).

However, Y-zeolite catalysts containing nickel-molybdenum have high yields of naphtha but low yields of kerosene and diesel required. Institut Francais du Petrole (IFP), a French company, modified Y containing a new type of nickel-molybdenum. Developed and used zeolite (trade name: HYC-642) catalyst to reduce the yield of naphtha and increase the yield of kerosene and diesel.

In particular, the above new type of modified Y-zeolite catalyst has a high activity of the catalyst and can change the conversion rate to 20-90% by varying the operating severity. Decomposition process) The conversion rate per pass was 50-90%, and if the main purpose of the production of lubricating base oil raw material (lubricating oil hydrocracking process), the conversion rate per pass could be adjusted to 20-30%. (November 1992 Petroleum Refining Meeting organized by Japan Petroleum Association)

When producing a base oil for lubricating oil, it is possible to replace an alumina supported with nickel-tungsten or the like or an amorphous silica-alumina supported with nickel-tungsten used as a catalyst in the conventional lubricating oil hydrolysis process with an IFP catalyst. That is, one IFP catalyst is an amorphous silica-alumina catalyst carrying nickel-molybdenum in the fuel oil hydrolysis process and an alumina carrying nickel-tungsten in the lubricating oil hydrolysis process or an amorphous silica-alumina catalyst carrying nickel-tungsten. Can do two functions.

Ii) prior art

Typically, a method of producing light fuel oil by hydrocracking is illustrated in FIGS. 1 and 2. US Chevron 1967 US Patent No. 3,308,055 shows that the hydrocracking process consisting of one reactor is disclosed as shown in FIG. That is, as shown in FIG. 1, the decompression gas oil is hydrocracked in a hydrolysis reactor R1, followed by atmospheric distillation in an atmospheric tower, and various fuel oils are separated. It is sent to the C oil tank or recycled to the hydrocracking reactor R1 for further decomposition.

However, the amorphous silica-alumina catalyst loaded with nickel-molybdenum, which is a catalyst used in the hydrocracking reactor of FIG. 1, is amorphous, and thus has low catalytic activity. Therefore, a high temperature is required and the conversion rate cannot be increased by more than 75% per pass. Since the throughput cannot be increased to more than about 20,000 B / D (Barrel per Day), a zeolite catalyst carrying a crystalline nickel-molybdenum or the like instead of the above amorphous catalyst (hereinafter referred to as “Ni-Mo / Y-zeolite catalyst”) will be developed. It became.

As shown in FIG. 2, the Ni-Mo / Y-zeolite catalyst for hydrocracking is charged to the hydrocracking reactor R2, and nitrogen and polynuclear aromatic compounds serving as catalyst poisons of the Ni-Mo / Y-zeolite catalyst are present in the reduced pressure gas oil. Therefore, in order to remove this, a hydrotreating reactor R1 is placed in front of the hydrolysis reactor R2, and an amorphous alumina catalyst loaded with nickel-molybdenum is charged to remove nitrogen with ammonia and the polynuclear aromatic compound is converted to lead-sensate. Some of the sulfur here is also removed with hydrogen sulfide.

Therefore, Figure 2 shows a one-step continuous hydrotreating-hydrolysis process, by increasing the decomposition activity of the Ni-Mo / Y-zeolite catalyst by removing the catalyst poison of the Ni-Mo / Y-zeolite catalyst from the hydrogenation reactor R1. A high conversion rate can be achieved and thus can handle 35,000 B / D of reduced pressure gas oil.

However, the process of Figure 2 has a hydrodynamic limit (Hydraulic Limitation) it is difficult to process the reduced pressure gas oil of more than 35,000 B / D in order to solve this problem in Figure 3 introduced a two-stage hydrolysis reactor R3.

In the two-stage hydrocracking process of FIG. 3, after decomposing the reduced-pressure gas oil into about 50% light oil in a batch process (Once Through Mode) in the first stage, the remaining hydrocracked residue oil is subjected to atmospheric distillation in a two-stage hydrolysis reactor R3. 50 to 70% of the residue is added and the remaining undecomposed hydrolysis residue is recycled to the atmospheric distillation column AT. The catalyst charged in the reactor R1 of FIG. 3 is the same as the catalyst charged in the R1 of FIG. 2, and the catalyst charged in the reactors R2 and R3 of FIG. 3 is the same as the catalyst charged in the reactor R2 of FIG. 2.

The process of FIG. 4 is a process of making a lubricating base oil by treating the hydrocracked residue oil (Hydrocrackate) generated in the process of FIG. 2 and then de-swapping in a catalytic dewaxing reactor R3 and stabilizing in a hydrogenation stabilizer R4. It is a process to obtain lubricating base oil.

However, the process of FIG. 4 is divided into a hydrolysis zone composed of a hydrotreating reactor R1 and a hydrocracking reactor R2, and a lubricating base oil zone consisting of a catalytic dewaxing reactor R3 and a hydrostable stabilization reactor R4.

Therefore, a separate hydrocracking zone and lubricating base oil area should be installed, which requires a lot of investment cost and complicated process. Specifically, the installation of lubricating base oil tank, addition of a reduced pressure distillation tower, and two independent recirculating hydrogen gas systems There are several inefficient problems in terms of investment cost, construction period, additional area and ease of operation.

In addition, in order to flexibly regulate production according to the change in demand for fuel oil and lubricating oil, a fuel oil hydrolysis zone and a lubricating base oil region are required, respectively.

The present invention is a two-stage hydrolysis process by adding a reactor R4 followed by a hydrolysis reactor R3 of two stages in the two-stage fuel oil hydrocracking process (FIG. 3) of IFP, and charging the dewaxing and hydrostable catalyst to the reactor R4. The combination of lubricating base oil process (catalyst dewaxing and hydrogenation stabilization process) enables simultaneous production of fuel oil and lubricating base oil, and allows the production rate to be flexibly adjusted according to the market situation.

In the combination of the hydrocracking process, the catalyst dewaxing process, and the hydrostable stabilization process, Ni-Mo / Y-zeolite, which is a catalyst of the hydrocracking process, must be present at a certain concentration or more to maintain activity because the metal must be present in the state of sulfide. 0.5%) hydrogen sulfide must be contained in the circulating hydrogen, and conversely, ZSM-5, which is a catalyst of the catalytic dewaxing process, loses activity due to hydrogen sulfide, and thus has a considerable difficulty in combining the hydrocracking zone and the lubricating base oil.

However, in the present invention, it has been found that the activity of the hydrocracking catalyst is maintained as it is and the activity of the dewaxing catalyst is hardly impaired when the concentration of hydrogen sulfide in the circulating hydrogen gas is in the range of 0.5% to 1.5%.

That is, by installing an amine absorption tower in the circulating hydrogen (not shown) to adjust the hydrogen sulfide concentration it was possible to combine the hydrocracking zone and the lubricating base oil region in a single process as shown in FIG.

The present invention is to enable the catalyst dewaxing process and the hydrogenation stabilization process in one reactor.

In addition, the present invention is to be able to perform the hydrocracking process, catalyst dewaxing process and hydrogenation stabilization process in one reactor.

1 is a schematic process diagram of hydrocracking consisting of a conventional one-stage one reactor.

Figure 2 is a schematic diagram of a continuous hydrotreatment-hydrolysis of a conventional one-stage two reactor.

Figure 3 is a hydrocracking schematic process diagram consisting of a conventional two stage three reactor. (Stage 1 :

Continuous Hydrotreatment-Hydrolysis Process, Step 2: Hydrolysis Process)

Figure 4 is a schematic process diagram of a continuous hydrotreatment / hydrocracking process (hydrogen decomposition zone) consisting of two conventional one-stage two reactors and a lubricant base oil zone to continuously catalyst dehydrogenation and hydrogenation of the lubricant base oil produced in the region.

Figure 5 is a schematic process diagram of the hydrolysis process that can produce fuel oil and lubricating base oil at the same time according to the present invention. (1 step: continuous hydrogenation and hydrocracking process,

Step 2: Hydrocracking / Lubrication Base Process (Catalyse Delamination and Hydrogenation Stabilization Process)

(Explanation of symbols for the main parts of the drawing)

AR (Atmospheric Residue): Atmospheric Residue VR (Vacuum Residue): Decompression Residue

AT (Atmospheric Tower): Atmospheric distillation tower VT (Vacuum Tower): Decompression distillation tower

R (Reactor): Reactor ST (Stripper): Stripper

CDW (Catalytic Dewaxing): Catalytic Dewaxing HF (Hydrofinishing): Hydrogenation Stabilization

LVGO (Light Vacuum Gas Oil): Light Pressure Gas Oil

MVGO (Middle Vacuum Gas Oil): Medium Pressure Gas Oil

HVGO (Heavy Vacuum Gas Oil): Heavy vacuum gas oil

The present invention will be described in detail.

As shown in FIG. 5, the present invention is a one-stage hydrolysis process consisting of two reactors (R1 and R2) and a two-stage hydrolysis process consisting of one hydrocracking reactor R3 and a catalyst dewaxing and a hydrostable catalyst in each layer. It consists of a lube base oil process consisting of one reactor R4 charged.

In addition, the present invention is a two-stage hydrolysis process consisting of two reactors (R1 and R2) and a two-stage hydrolysis process consisting of one hydrocracking reactor R3 and hydrolysis, catalyst dewaxing and hydrostable catalyst as shown in FIG. It consists of a lubricating base oil process consisting of one reactor R4 filled with each bed.

Atmospheric Residue (AR: Atmospheric Residue) is distilled under reduced pressure in a vacuum tower (VT1: Vacuum Tower) to obtain a reduced pressure gas oil, and this vacuum gas oil (VGO: Vacuum Gas Oil) is first introduced into a one-step hydrocracking process.

The first hydrotreating reactor (R1) was charged with an amorphous alumina catalyst loaded with nickel-molybdenum to remove nitrogen, which is a catalyst poison of the modified Y-zeolite loaded with nickel-molybdenum, by converting it into ammonia, and converting the polynuclear aromatic compound into a lead-sen group. Let's do it. Part of the sulfur is also converted to hydrogen sulfide and removed.

The second reactor R2 was charged with a modified Y-zeolite catalyst supported by nickel-molybdenum (trade name HYC-642, manufactured by IFP, France) to hydrocrack the hydrogenated vacuum gas oil, followed by AT (Atmospheric Tower). By distillation under atmospheric pressure, it is separated into fuel oil components such as LPG, naphtha, kerosene, and diesel oil and hydrocracked residue oil (lubricating base oil).

The fuel oil component is sent to the fuel storage tank and the hydrocracked residue oil is sent to the second stage hydrocracking reactor R3 for hydrocracking again. The catalyst of R3 is the same as that of R2. Effluent from the hydrocracking reactor R3 is introduced into the lube base oil process.

The lubrication base oil process consists of one reactor (R4) consisting of two or three layers and is characterized by catalyst dewaxing and hydrostable stabilization (two layers), or hydrocracking, catalyst stripping and hydrostable stabilization (three layers). Do this.

In the case of two layers, ZSM-5 catalyst, which is a dewaxing catalyst, is charged in the upper layer, and an amorphous alumina catalyst in which nickel-tungsten, a hydrogenation stability catalyst is supported, in the lower layer; A modified Y-zeolite catalyst (trade name HYC-642 manufactured by IFP, France), a middle layer of the dewaxing catalyst ZSM-5 catalyst, and a bottom layer of the amorphous alumina catalyst carrying nickel-tungsten, a hydrogenation stabilization catalyst.

The effluent from R4 is introduced into a stripper, part of which is sent to the atmospheric distillation tower (AT) and the remainder to the vacuum tower VT2 to obtain various types of lubricant base oils.

In the present invention, the hydrogen sulfide concentration is maintained at 0.5 to 1.5 vol% by circulating hydrogen in a single loop hydrogen circulation system and adjusting the amine absorption tower throughout all processes.

Example 1

The physical properties of the vacuum gas oil obtained by distilling the atmospheric residual oil (AR: Atmospheric Residue) in the vacuum distillation column VT1 under reduced pressure are shown in Table 1.

Physical properties of vacuum gas oil Properties Reduced pressure gas oil Viscosity, @ 40 ° C., cSt 32.24 -Viscosity index 72 Sulfur, wt% 2.51 Nitrogen, wtppm 600 Aromatic compounds, wt% 51.3

The vacuum gas oil was first introduced into a one-step hydrocracking process. In the first hydrotreating reactor R1, the reduced-pressure gas oil was carried out in the presence of a nickel-molybdenum-supported alumina catalyst at a temperature of 390 ° C, a pressure of 158 kg _f / cm ² and a liquid hourly space velocity of 1.5hr ^-1 . Hydrotreated.

The effluent (hydrogenated reduced pressure gas oil) from R1 was introduced into a hydrocracking reactor R2 to give a temperature of 383 ° C in the presence of a modified Y-zeolite catalyst (HYC-642 from IFP, France) supported by nickel-molybdenum and Hydrolysis was carried out under a pressure of 158 kg _f / cm ² and a liquid space velocity of 3.0 hr ^-1 .

The effluent from R2 is introduced into the atmospheric distillation tower AT together with the light effluent from the stripper, and it is distilled under atmospheric pressure to separate fuel components such as LPG, naphtha, kerosene, and diesel oil into the storage tank, and to add hydrolyzed residue oil (lubricating base oil). Was sent to a hydrolysis reactor R3.

Physical properties of the hydrocracked residue oil are shown in Table 2.

Properties of Hydrocracked Residual Oil Hydrolysis Residual Oil Conversion rate, wt% 65.9 Properties Viscosity, @ 40 ° C., cSt 25.83 -Viscosity index 131 Pour point, ℃ +38.0 Sulfur, wt% 0.0036 Nitrogen, wtppm One Aromatic compounds, wt% 5.43

In this reaction, the aromatics were converted to lead-sensing compounds, which decreased from 51.3 wt% to 5.43 wt% in reduced pressure gas oil, increasing the viscosity index from 72 to 131.

The hydrocracked residue oil was modified in a two-stage hydrocracking reactor R3 with a nickel-molybdenum-modified Y-zeolite catalyst at a temperature of 335 ° C, a pressure of 158kg _f / cm ² , and a space velocity of 1.1hr ^-1 (French IFP 312 cc of the brand name HYC-642) was hydrogenated again.

The hydrolyzed R3 effluent was re-hydrogenated on the upper layer of nickel-molybdenum-modified Y-zeolite catalyst (88 HYC-642, manufactured by IFP, France) and in the middle layer, ZSM- 62cc of 5 catalysts and 125cc of alumina catalyst loaded with nickel-tungsten, a hydrogenation stabilization catalyst, were introduced into the lubricating base oil reactor R4 packed with hydrogenation, dewaxing, and hydrogenation under the operating conditions shown in Table 3. In addition, the amine absorption tower was adjusted to maintain 1.5 vol% of hydrogen sulfide in the circulating hydrogen.

Operating conditions of two-step continuous hydrocracking and hydrocracking / catalytic dewaxing / hydrogenation stabilization Hydrocracking Catalyst (R3) Hydrocracking Catalyst (R4) Catalyst Dropping Catalyst (R4) Hydrogenation Stabilization Catalyst (R4) Reaction pressure, kg _f / cm ² 158 158 158 158 LHSV, hr ^-1 1.1 1.9 5.5 2.8 WABT, ℃ 335 335 360 360

The hydrocracking reaction of the reactor R4 was an adiabatic exothermic reaction and thus a temperature rise occurred in the hydrocracking reaction and the hydrostable stabilization reaction. The space velocity becomes large when the amount of the catalyst is small and becomes small when the amount of the catalyst is large, and depends on the amount of catalyst in each layer.

The effluent from R4 was sent to the stripper, and the light effluent was sent to the atmospheric distillation tower AT, and the rest of the lubricant oil (300 ° C.) was sent to the vacuum distillation tower VT2 to obtain 60N and 100N of lubricating base oil as shown in Table 4.

Examples of Lubricant Base Oils Produced from a Two-stage Continuous Hydrolysis and Hydrolysis / Catalysis Dewaxing / Hydration Stabilization Process Lubricant oil (300 ℃ +) 60N 100N 1. Yield of lube base oil, wt% 14.8 2.9 8.9 2. Properties of Lubricant Oil Viscosity, @ 40 ° C., cSt 22.10 7.333 20.17 -Viscosity index 105 90 104 Pour point, ℃ -20.0 -40 or less -20.0

The property values in the above tables are the values when the process reached Steady State.

Example 2

The physical properties of the vacuum gas oil obtained by distilling the atmospheric residual oil (AR: Atmospheric Residue) in the vacuum distillation column VT1 under reduced pressure are shown in Table 5.

Physical properties of vacuum gas oil Properties Reduced pressure gas oil Viscosity, @ 40 ° C., cSt 32.24 -Viscosity index 72 Sulfur, wt% 2.51 Nitrogen, wtppm 600 Aromatic compounds, wt% 51.3

The vacuum gas oil was first introduced into a one-step hydrocracking process. In the first hydrotreating reactor R1, the reduced-pressure gas oil was carried out in the presence of a nickel-molybdenum-supported alumina catalyst at a temperature of 390 ° C, a pressure of 158 kg _f / cm ² and a liquid hourly space velocity of 1.5hr ^-1 . Hydrotreated.

The effluent (hydrogenated reduced pressure gas oil) from R1 was introduced into a hydrocracking reactor R2 to give a temperature of 383 ° C in the presence of a modified Y-zeolite catalyst (HYC-642 from IFP, France) supported by nickel-molybdenum and Hydrolysis was carried out under a pressure of 158 kg _f / cm ² and a liquid space velocity of 3.0 hr ^-1 .

The effluent from R2 is introduced into the atmospheric distillation tower AT together with the light effluent from the stripper, and it is distilled under atmospheric pressure to separate fuel components such as LPG, naphtha, kerosene, and diesel oil into the storage tank, and to add hydrolyzed residue oil (lubricating base oil). Was sent to a hydrolysis reactor R3.

Physical properties of hydrocracked residue oil are shown in Table 6.

Properties of Hydrocracked Residual Oil Hydrolysis Residual Oil Conversion rate, wt% 65.9 Properties Viscosity, @ 40 ° C., cSt 25.83 -Viscosity index 131 Pour point, ℃ +38.0 Sulfur, wt% 0.0036 Nitrogen, wtppm One Aromatic compounds, wt% 5.43

In this reaction, the aromatics were converted to lead-sensing compounds, which decreased from 51.3 wt% to 5.43 wt% in reduced pressure gas oil, increasing the viscosity index from 72 to 131.

The above hydrocracked residue oil was modified in a two-stage hydrocracking reactor R3 at a temperature of 371 ° C., a pressure of 158 kg _f / cm ² , and a modified Y-zeolite catalyst supported by nickel-molybdenum at a space velocity of 1.5 hr ⁻¹ (French IFP). 500 cc of the brand name HYC-642) was further hydrolyzed.

Hydrogenated R3 effluent was introduced again into the lubricating base oil reactor R4 filled with 227 cc of catalyst desorption catalyst ZSM-5 catalyst on the upper layer and alumina catalyst 278 cc loaded with nickel-tungsten, hydrogenation stabilizer on the lower layer. Waxing and hydrogenation stabilization were carried out under the operating conditions of 7. In addition, hydrogen sulfide in circulating hydrogen was maintained at 1.5 vol% by adjusting the amine absorption tower.

Operating conditions of two-step continuous hydrocracking and catalyst dewaxing / hydrogenation stabilization Hydrocracking Catalyst (R3) Catalyst Dropping Catalyst (R4) Hydrogenation Stabilization Catalyst (R4) Reaction pressure, kg _f / cm ² g 158 158 158 LHSV, hr ^-1 1.5 3.3 2.7 WABT, ℃ 371 320 290

The dewaxing catalyst in the upper layer of the R4 reactor and the hydrogenation stabilization catalyst were charged in the lower layer. The temperature of each catalyst layer was controlled by hydrogen injection for cooling between the layers.

The effluent from R4 was sent to the stripper, and the light effluent was sent to the atmospheric distillation tower AT, and the remaining lubricant oil (360 ° C. +) was sent to the vacuum distillation tower VT2 to obtain 60N and 150N of lube base oil as shown in Table 8.

Examples of Lubricant Base Oils Produced from a Two-Stage Continuous Hydrolysis and Catalytic Desorption / Hydration Stabilization Process Lubricant oil (300 ℃ +) 60N 150N 1. Yield of lube base oil, wt% 10.0 3.8 3.8 2. Properties of Lubricant Oil -Color, Saybolt +30 +30 +30 Viscosity, @ 40 ° C., cSt 9.94 6.962 32.02 -Viscosity index 102 96 109 Pour point, ℃ -27.0 -36.0 -17.0 Aromatic, wt% 0.16 0.12 0.16 -Thermal stability, 12/24 hours L1.0BC / L1.5BC L1.0BC / L1.5BC L1.0BC / L2.0BC -UV stability, 24/48 hours L0.5BC / L0.5BC L0.5BC / L0.5F L1.5BC / L1.5BC

The property values in the above tables are the values when the process reached Steady State.

The present invention is a two-stage hydrolysis process by adding a reactor R4 followed by a two-stage hydrolysis reactor R3 in IFP's two-stage fuel oil hydrocracking process (FIG. 3) and filling the reactor R4 with a dewaxing catalyst and a hydrostable catalyst. Combination with the lube base oil process (catalyst dewaxing and hydrogenation stabilization process) was able to produce fuel oil and lube base oil at the same time, and the production ratio could be flexibly adjusted according to the market situation.

On the other hand, by combining the two-stage hydrolysis process and the lube base oil process (desoldering / hydrogenation stabilization) in a single process, the additional installation of the lubricating oil raw material tank, atmospheric pressure and reduced pressure distillation tower is reduced, and two independent circulating hydrogen systems are reduced to one circulating hydrogen system. Investment costs could be reduced and production could be increased by reducing operating costs and increasing operating days.

Claims (6)

Atmospheric Residue (AR: Atmospheric Residue) was distilled under reduced pressure in VT1 (Vacuum Tower) to obtain vacuum gas oil (VGO), which was introduced into a hydrotreating reactor R1, hydrotreated and the effluent from R1 Hydrolysis is introduced into the hydrocracking reactor R2, and the effluent from R2 is introduced into the AT (Atmospheric Tower) with the light effluent from the stripper ST, and is distilled under atmospheric pressure to separate fuel components from the AT effluent into the storage tank. The remaining hydrocracked residue oil (lubricating base oil) is sent to the second stage hydrocracking reactor R3 for second hydrocracking, and the effluent from R3 is subjected to catalyst dewaxing and hydrostable stabilization and sent to stripper ST. In the method for producing a lubricant base oil by sending to the AT and the remaining lubricant oil fraction to a vacuum distillation column VT2, two stage hydrocracking reactor R3, followed by catalyst dropping and hydrogenation A process for producing an advanced lubricating base oil, characterized in that a lubricating base oil reactor (R4) capable of continuously purifying in one reactor and an amine absorption tower are further installed to control the hydrogen sulfide concentration. The method of claim 1, wherein the upper layer of the lubricating base oil reactor R4 is filled with a hydrolysis catalyst, a middle dewaxing catalyst, and a lower layer with a hydrogenation stabilization catalyst. The catalyst of the hydrocracking catalyst layer is a modified Y-zeolite (trade name HYC-642 manufactured by IFP, France) supported by nickel-molybdenum, the catalyst of the dewaxing catalyst layer is a ZSM-5 catalyst and a hydrostable catalyst layer. The catalyst is a method for producing a high lubricating base oil, characterized in that the nickel-tungsten-supported amorphous alumina catalyst. The method of claim 1, wherein the upper layer of the lubricant base oil reactor R4 is filled with a dewaxing catalyst, and the lower layer is filled with a hydrogenation stabilized catalyst. The method of claim 4, wherein the catalyst of the dewaxing catalyst layer is a ZSM-5 catalyst and the catalyst of the hydrogenation stabilization catalyst layer is an amorphous alumina catalyst carrying nickel-tungsten. The preparation of the high-grade lubricating base oil according to claim 1, 2, 3, 4 or 5, wherein the amine absorption tower is adjusted to maintain the hydrogen sulfide concentration in the circulating hydrogen at 0.5 to 1.5 vol%. Way.