KR20060130675A - Process to continuously prepare two or more base oil grades and middle distillates - Google Patents

Abstract

Process to prepare simultaneously two or more base oil grades and middle distillates from a de-asphalted oil or a vacuum distillate feed or their mixtures by performing the following steps: (a) hydrocracking the feed, thereby obtaining an effluent; (b) distillation of the effluent as obtained in step (a) into one or more middle distillates and a residue boiling substantially above 340°C; (c) separating, by means of a further distillation step said residue into a light base oil precursor fraction and a heavy base oil precursor fraction; (d) reducing the pour point of each separate base oil precursor- fraction iri"two simultaneously and parallel operated catalytic dewaxing reactors obtaining a first and second dewaxed oil; (e) hydrotreating the first dewaxed oil as obtained when dewaxing the heavy base oil precursor fraction in step (d); (f) isolating from the second dewaxed oil from the light base oil precursor fraction from step (d) and the hydrotreated oil from step (e) two or more base oil grades.

Description

Process to continuously provide two or more base oil grades and heavy distillates {PROCESS TO CONTINUOUSLY PREPARE TWO OR MORE BASE OIL GRADES AND MIDDLE DISTILLATES}

The present invention relates to a process for continuously providing at least two base oil grades and heavy distillates.

WO-A-0250213 describes a process in which other base oils are made in a so-called blocking manner. In this process, the bottom fraction of the fuel hydrocracking process, which produces heavy distillate as a product, is separated into various base oil precursor fractions. This fraction is dewaxed after using a platinum-ZSM-5 based catalyst.

WO-A-9718278 discloses a process in which four base oil grades, for example 60N, 100N and 150N, are provided starting from the bottom fraction of a fuel hydrocracker. In this process, the bottom fraction is divided into five fractions in vacuum distillation, and the four heavy fractions of these five fractions are further subjected to different base oil grades by first performing catalytic dewaxing and then hydrotreating. Is processed.

WO-A-02 / 50213 discloses a so-called blocking process for preparing different base oil grades from the bottom fraction of a fuel hydrocracking process.

The disadvantage of this process is that the process is not continuous. That is, base oil grades are made sequentially, not simultaneously. This requires storage for the intermediates obtained while sorting the hydrocracker bottom and waiting for the catalyst to be dewaxed. Another drawback is the mode switch due to the cooling and heating of the equipment causing corrosion of the equipment. The mode switch also causes a medium fail product each time a new grade is processed. Such undesirable debris must be reprocessed or disposed of.

EP-A-649896 discloses a process for providing a residue comprising base oil by a process comprising a hydroprocessing step and a hydrocracking step in a heavy petroleum feedstock. The hydroprocessing step produces a product from which heavy distillate and bottoms fractions (residues) are obtained. This bottom fraction is then a solvent dewaxed to a single base oil grade.

EP-A-0 272 729 discloses a process for producing lubricating base oils in which the flashed distillate produced by the residue conversion process is fed to a hydrocracking unit. Effluent from the hydrocracking unit is fed to the dewaxing unit of the catalyst, after which the optionally completely dewaxed stream is subjected to hydroprocessing.

WO-A-9723584 discloses a process in which the bottoms fraction of a fuel hydrocracker is subjected to a dewaxing stage of the catalyst. The dewaxed oil is partly recycled to the hydrocracking stage and partially lubricated base oil is obtained.

A disadvantage of the process described in WO-A-9723584 is that a large pour point distribution occurs when two or more base oil grades are separated from the dewaxed oil. As a result, the low viscosity base oil grade has a very low pour point. This pour point must be eliminated, or the difference from the desired value indicates a loss of production of the low viscosity base oil grade.

One object of the present invention is to provide a process which can simultaneously provide two or more base oil grades and whose respective pour points are closer to the desired values.

Another object of the present invention is to provide a process of another method.

The following process achieves one or more of these or other objects.

A process for simultaneously providing two or more base oil grades and heavy distillates from deasphalted oil or vacuum distillate feedstock or mixtures thereof,

(a) hydrocracking the feedstock to obtain emissions;

(b) distilling the effluent obtained in step (a) into a boiling residue and at least one heavy distillate substantially above 340 ° C.,

(c) separating the residue into a light base oil precursor fraction and a heavy base oil precursor fraction by a subsequent distillation step,

(d) lowering the pour point of each base oil precursor fraction separated in the dewaxing reactor of the catalyst operated at the same time and in parallel to obtain a first dewaxed oil and a second dewaxed oil,

(e) hydroprocessing the first dewaxed oil obtained by dewaxing the heavy base oil precursor fraction in step (d),

(f) separating at least two base oil grades from the second dewaxed oil, the light base oil precursor fraction from step (d) and the hydrogenated oil from step (e).

When treating in accordance with the present invention, it is possible to continuously provide two or more base oil grades, and at the same time reduce the hydrotreatment capacity, since heavy grades requiring subsequent hydrogenation treatment are carried out in step (e) above. Because. In addition, any product that has eliminated the pour point can be avoided because two parallel dewaxing reactors can be operated so that the high and low viscosity base oil grade pour point approaches the desired value. Elimination of any pour point represents a grade of production loss with a pour point lower than the desired pour point.

The feedstock to step (a) can be any conventional natural mineral oil feedstock to the hydrocracking plant. Such feedstocks are vacuum light oil or heavy distillate fractions obtained when distilling atmospheric residues of natural petroleum feedstocks in near vacuum. The deasphalted oil obtained when deasphalting the residue obtained in the vacuum distillation is also used as feedstock. Light cycle oils and heavy cycle oils obtained in the fluid catalytic cracking (FCC) process, such as the rich aromatic extracts obtained during solvent extraction in conventional base oil treatments, are also used as feedstocks. Mixtures of the feedstocks described above and optionally other hydrocarbon feedstocks are also suitable as feedstocks. In addition to the feedstock, another optional hydrocarbon feedstock, preferably 2-30 wt% of the feedstock in step (a), is paraffin wax obtained in the Fischer-Tropsch process. The feedstock to step (a) is preferably composed of natural mineral derived feedstock.

Step (a) is carried out at conversion levels 15 to 90 wt%. The conversion is expressed in wt% of the fraction of the feedstock boiling above 370 ° C., which is converted to a boiling product below 370 ° C. The main products boiling below 370 ° C are gasoline, kerosene and diesel. Examples of hydrocracking processes suitable for carrying out step (a) are described in EP-A-699225, EP-A-649896, WO-A-9718278, EP-A-705321, EP-A-994173, US-A-4851109 It is.

As operating conditions of the single stage hydrocracking process, preferably a temperature of 350 to 450 ° C., a hydrogen pressure of 9 to 200 MPa, more preferably a hydrogen pressure of 11 MPa or more, and an amount of 0.1 to 10 Kg oil per liter of catalyst per hour ( Kg / L / hr) weight time space velocity (WHSV), preferably 0.2-5 Kg / L / hr weight time space velocity, more preferably 0.5-3 Kg / L / hr weight time space velocity, And a ratio of hydrogen to oil of 100 to 2,000 liters of hydrogen per liter of oil.

Preferably the hydrocracker is operated in two stages including the hydrocracking step after the main hydroprocessing step. In the hydrotreating step, nitrogen and sulfur are significantly removed, the aromatics are sufficiently saturated with naphthenes, and some of the naphthenes are converted to paraffins by a ring opening reaction. In order to improve the production of larger viscous grade base oils, the fuel hydrocracking plant is characterized by (i) hydrotreating the hydrocarbon feedstock with a feedstock conversion of less than 30 wt%, preferably 15-25 wt%, as indicated above. Step (i) in the presence of a hydrocracking catalyst at a conversion level where (ii) the conversion of steps (i) and (ii) is from 15 to 90 wt% and preferably from 40 to 85 wt%. More preferably it is operated by hydrocracking the product.

As operating conditions of the single stage hydrocracking process, preferably a temperature of 350 to 450 ° C., a hydrogen pressure of 9 to 200 MPa, more preferably a hydrogen pressure of 11 MPa or more, and an amount of 0.1 to 10 Kg oil per liter of catalyst per hour ( Kg / L / hr) weight time space velocity (WHSV), preferably 0.2-5 Kg / L / hr weight time space velocity, more preferably 0.5-3 Kg / L / hr weight time space velocity, And a ratio of hydrogen to oil of 100 to 2,000 liters of hydrogen per liter.

The operating conditions of the hydrocracking step carried out in combination with the hydroprocessing step are preferably temperatures of 300 to 450 ° C., hydrogen pressures of 9 to 200 MPa, more preferably hydrogen pressures of at least 11 MPa, 0.1 per liter of catalyst per hour Weight time space velocity (WHSV) of from 10 Kg oil amount (Kg / L / hr), preferably weight time space velocity of 0.2 to 5 Kg / L / hr, more preferably 0.5 to 3 Kg / L / hr Weight time space velocity, and the ratio of hydrogen to oil of 100 to 2,000 liter hydrogen per liter of oil.

The residue provided by the process described above has a very low sulfur, typically less than 250 ppmw or less than 150 ppmw, and a very low nitrogen content, typically less than 30 ppmw. The residue is preferably a full range residue.

By combining the hydrotreatment step and hydrocracking step as described above, a large amount of base oil of a larger viscosity grade, such as heavy machine oil grade, and residues producing acceptable quality for the viscosity index are obtained. Was found. In addition, this process yields sufficient amounts of gasoline, kerosene and diesel. Thus, a fuel hydrocracking process is achieved in which products and residues from gasoline to diesel are obtained at the same time, and the residue has the potential to produce base oil grades of heavy machinery oils. Accordingly, the viscosity index of the base oil grade is preferably 95 to 120, and can produce a base oil having a viscosity index according to the API Group II specification.

In the hydrotreatment step (i), the residue and hence base oil grade viscosity index increases with the conversion of the hydrotreatment step. By carrying out the hydrotreatment step at a higher conversion level greater than 30 wt%, a viscosity index value of 120 or more base oil can thus be achieved. However, a disadvantage of the high conversion of step (i) is that the yield of heavy machine oil fractions is undesirably low. By carrying out step (i) at the conversion level described above, API II heavy machinery oil grade base oils can be obtained in the desired amounts. The minimum conversion in step (i) is thus determined by the desired viscosity index of 95 to 120 of the base oil grade, and the maximum conversion in step (i) is determined by the minimum allowable yield of heavy machine oil grade. .

The prehydrogenation step is typically carried out using the same conditions as in the examples described in the above-mentioned publications relating to catalysts and hydrocracking. Suitable hydrotreating catalysts typically suitably comprise a metal hydrogenation component, for example Group IVB or Group VIII metals such as cobalt-molybdenum, nickel-molybdenum, in a porous support such as silica-alumina or alumina. The hydrotreating catalyst preferably contains no zeolite material or contains very small amounts of less than 1 wt%. Examples of preferred hydrotreatment catalysts are commercially available ICR 106, ICR 120, Criterion Catalyst Co., 244, 411, DN-120 from Chevron Research and Technology Co. , DN-180, DN-190 and DN-200, TK-555 and TK-565 from Haldor Topsoe A / S, HC-K, HC-P, HC-R and HC-T from UOP , KF-742, KF-752, KF-846, KF-848 STARS and KF-849 from AKZO Nobel / Nippon Ketjen, HR-438 / from Procatalyse SA 448

The hydrocracking step is preferably a catalyst comprising a zeolite having a large acid pore in a porous support having an added metal hydrogenation / dehydrogenation function. Metals having a hydrogenation / dehydrogenation function are preferably Group VIII / VIB metal combinations such as nickel-molybdenum and nickel-tungsten. The support is preferably a porous support, for example silica-alumina and alumina. As explained above, when the hydrocracking plant is run at the desired conversion level, it is advantageous that the minimum amount of zeolite is contained in the catalyst in order to obtain a high yield of heavy mechanical oil fraction in the full range of residues. It is preferred that more than 1 wt% zeolite is contained in the catalyst. Examples of preferred zeolites are zeolite X, Y, ZSM-3, ZSM-18, ZSM-20, and zeolite Y which are the most preferred zeolite β. Examples of preferred hydrocracking catalysts are commercially available ICR 220 and ICR 142 from Chevron Research and Technology Co., Z-763, Z-863, Z-753 of Zeolist International. , Z-703, Z-803, Z-733, Z-723, Z-673, Z-603 and Z-623, TK-931 from Haldor Topsoe A / S, DHC-32 from UOP , DHC-41, HC-24, HC-26, HC-34 and HC-43, KC2600 / 1, KC2602, KC2610, KC2702 and KC2710, Procatal from Akzo Nobel / Nippon Ketjen HYC 642 and HYC 652 from Pro catalyse SA.

The effluent of the hydrocracker is separated into one or more fuel fractions and residues mentioned above. Overwhelmingly boiling residues above 340 ° C. are used as feedstock to step (c). Overwhelmingly boiling above 340 ° C. means boiling above 340 ° C. above 80 wt%, preferably above 90 wt%. Since a significant fraction of the residues boil in the diesel range, most of the diesel is recovered after dewaxing with good cold flow properties. Preferably, 10 to 40 wt% dewaxed oil obtained in this process is boiled in heavy diesel oil at 350 to 400 ° C. Of course, it should also be noted that at low points a boiling diesel fraction is obtained in step (c).

The final boiling point of the residue is determined in part by the final boiling point of the feedstock to step (a) and may be above 700 ° C., a value which cannot be determined by standard test methods.

The optional fraction of the residue obtained in step (b) is recycled to step (a) as in the example described in publication EP-A-0994173 referenced herein. Optionally, the residue is recycled only to the hydrocracking step of step (a) as in the example described in publication EP-B-0699225 referenced herein. Less than 15 wt% residue is preferably recycled to step (a), more preferably no residue is recycled to step (a). It was found that API Group II base oils were supplied with good quality without such recycling.

In step (c), the feedstock is separated by fractional distillation into a light base oil precursor fraction and a heavy base oil precursor fraction and optionally a vacuum gas oil fraction. Although no vacuum gas oil is separated from the light base oil precursor fraction, it is preferred that it remain mixed with the fraction so as to be waxed in step (d). Fractional distillation is preferably carried out at a reduced pressure, more preferably vacuum fractional distillation is carried out at a pressure of 0.01 to 0.3 bara. The 10 wt% recovery point of the heavy base oil precursor fraction obtained in step (c) is preferably 420 to 550 ° C, more preferably 440 to 520 ° C.

The feedstock to step (d) comprises the base oil precursor fraction obtained in step (c). Optionally partially partially isomerized paraffin wax boiling in the boiling range of the heavy or light base oil precursor fraction is contained in a mixture with the light base oil precursor fraction. This paraffinic product is also described as wax raffinate obtained in a Fischer-Tropsch or gas-liquid process. Such wax raffinate is supplied according to the process described in publication WO-02070630, which is incorporated herein by reference.

Optionally, the precious metal protective layer is located immediately upstream of the dewaxing catalyst layer in the dewaxing reactor of step (d) in order to reduce the levels of sulfur and in particular the nitrogen component. Such protective layers are particularly useful in dewaxing reactors in which heavy base oil precursor fractions proceed. Examples of such processes are described in WO-A-9802503, which is incorporated herein by reference.

The dewaxing of the catalyst in the reactor operated in parallel in step (d) can be carried out by any process in which the pour point of the catalyst and hydrogen containing base oil fraction is reduced. Preferably, the pour point is reduced to at least 10 ° C, more preferably reduced to at least 20 ° C. Preferred dewaxing catalysts are heterogeneous catalysts which comprise molecular sieves and which are optionally bonded with a metal having a hydrogenation function such as Group VIII metal. Molecular sieves, and more preferably, mesoporous zeolites have excellent catalytic ability to reduce the pour point of the base oil fraction under dewaxing conditions of the catalyst. Zeolites of medium porosity are preferably pore diameters of 0.35 to 0.8 nm. Preferred mesoporous zeolites are ZSM-5, ZSM-12, ZSM-22, ZSM-23, SSZ-32, ZSM-35 and ZSM-48. Another preferred group of molecular sieves is silica-alumina phosphate (SAPO) material, with SAPO-11 being the most preferred as an example described in US-A-4859311. ZSM-5 may optionally be HZSM-5 in the absence of any Group VIII metal. Other molecular sieves are preferably used in combination with the added Group VIII metal. Preferred examples of Group VIII metals are nickel, cobalt, platinum and palladium. Examples of possible combinations are Ni / ZSM-5, Pt / ZSM-23, Pd / ZSM-23, Pt / ZSM-48 and Pt / SAPO-11. Further details and examples of preferred molecular sieves and dewaxing conditions are described by way of example in WO-A-9718278, US-A-5053373, US-A-5252527 and US-A-4574043.

The process according to the invention makes it possible to continuously provide base oils using a dewaxing catalyst, which dewaxing catalyst is relatively large when the full range residues are treated as in the examples described in WO-A-9723584. Pour point distribution. By using the present invention, such a large pour point distribution can be avoided while using the relatively low dewaxing catalyst. An example of a catalyst exhibiting a relatively large pour point distribution is a ZSM-5 based catalyst. Thus ZSM-5 based catalysts are advantageously applied in the present invention. The process also makes it possible to use different dewaxing catalysts in reactors operating in parallel, and the catalysts can be adapted to their respective feedstocks.

The dewaxing catalyst preferably also comprises a binder. The binder may comprise synthetic or naturally occurring (inorganic) materials, such as mud, silica and / or metal oxides. Examples of naturally occurring muds are montmorillonite and kaolin. The binder is preferably a porous binder material, examples of the oxides include alumina, silica-alumina, silica-magnesia, silica-zirconia, silica-toria, silica-berilia, silica-titania, as well as examples of ternary compositions, Silica-alumina-toria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia. More preferably, a weak acid resistant binder material is used which is essentially free of alumina. Examples of such binder materials are silica, zirconia, titanium dioxide, germanium dioxide, boria and mixtures of two or more of these examples. The most preferred binder is silica.

Preferred types of dewaxing catalysts include weakly acidic oxide binder materials that are essentially free of alumina as described above and intermediate zeolite crystallites as described above, and the surface of the aluminosilicate zeolite microcrystals The no-silicate zeolite microcrystals have been modified by providing surface dealumination treatment. Preferred dealumination treatment is to contact the extrudate of the bind and zeolite with an aqueous solution of fluorinated silicate as described, for example, in US-A-5157191. Examples of preferred dewaxing catalysts as described above include silica bonds and dealuminated Pt / ZSM-5, silica bonds and dealumination Pt / ZSM, as described in WO-A-200029511 and EP-B-832171. -23, silica bonds and dealuminated Pt / ZSM-12, and silica bonds and dealuminated Pt / ZSM-22.

Dewaxing conditions of the catalyst are known in the art and are typically temperatures of 200 to 500 ° C., preferably temperatures of 250 to 400 ° C., hydrogen pressures of 10 to 200 bar, and amounts of 0.1 to 10 Kg oil per liter of catalyst per hour Weight time space velocity (WHSV) of (Kg / L / hr), preferably weight time space velocity of 0.2 to 5 Kg / L / hr, more preferably weight time space velocity of 0.5 to 4 Kg / L / hr And the ratio of hydrogen to oil of 100 to 2,000 liters of hydrogen per liter of oil. The weight time space velocity (WHSV) in the dewaxing stage of the catalyst where the light base oil precursor fraction is treated is preferably higher than the WHSV in the dewaxing stage of the heavy base oil precursor fraction. More preferably, the WHSV of the dewaxing stage of the light base oil precursor fraction is 1-5 Kg / L / hr.

If the dewaxing step and the hydrofinishing step are carried out in a series of reactions, the pressure levels in both steps are preferably the same. Since higher pressures are preferred in the hydrotreating step to obtain base oils with desirable properties, it is preferable that the dewaxing step is also performed at a higher pressure, although more selective dewaxing can be carried out at lower pressures. If no hydrotreating step is required as found for dewaxed oils obtained from light base oil precursor fractions to provide, for example, spindle oil base oil grades, lower catalyst dewaxing pressures can be advantageously applied. Preferred pressures are 15 to 100 bar, more preferably 1.5 to 6.5 MPa.

The hydrotreatment step (e), which is a hydrotreating step, is also a step of improving the quality of the dewaxed fraction. In this step, olefins in the lubricating oil range are saturated, heteroatoms and pigments are removed, and residual aromatics are saturated if the pressure is high enough. Preferably, the conditions are selected to obtain a base oil grade comprising more than 95 wt% saturates, and more preferably so that the base oil comprises more than 98 wt% saturates. The hydrotreating step is preferably carried out in a series of reactions of the dewaxing step of the heavy base oil precursor fraction.

The hydrotreating step is preferably carried out at a temperature of 230 to 380 ° C., at a total pressure of 1 to 25 MPa and preferably at least 10 MPa and more preferably 12 to 25 MPa. WHSV (weight time space velocity) is 0.3 to 10 Kg oil amount (Kg / L / hr) per liter of catalyst per hour.

The hydrotreating or hydrogenation catalyst is preferably a supported catalyst comprising dispersed Group VIII metal. Possible Group VIII metals are cobalt, nickel, palladium and platinum. Cobalt and nickel containing catalysts may also include Group VIB metals, preferably molybdenum and tungsten.

Preferred carriers or supports are weakly acidic amorphous oxides. Examples of preferred amorphous oxides are inorganic oxides such as alumina, silica, titania, zirconia, boria, silica-alumina, fluorinated alumina, fluorinated silica-alumina and mixtures of two or more thereof.

Preferred hydrogenation catalysts comprise a catalyst comprising one or more of 1 to 25 wt%, preferably 2 to 15 wt% of nickel (Ni) and cobalt (Co) calculated as elements relative to the total weight of the catalyst, and the total of the catalyst 5 to 30 wt%, preferably 10 to 25 wt%, of at least one Group VIB metal component calculated as elements by weight. Examples of preferred nickel-molybdenum containing catalysts are KF-847, KF-8010 (AKZO Nobel), M-8-24, M-8-25 (BASF), C-424, DN-190, HDS-3 HDS-4 (Criterion). Examples of preferred nickel-tungsten containing catalysts are NI-4342, NI-4352 (Engelhard), and C-454 (Criterion). Examples of preferred cobalt-molybdenum containing a catalyst are KF-330 (AKZO Nobel), HDS-22 (Criterion), HPC-601 (Engelhard).

For the hydrocracked feedstock containing small amounts of sulfur in the present invention, platinum containing the catalyst, more preferably platinum containing the catalyst and palladium are used. The total amount of Group VIII noble metal component present in the catalyst is 0.1 to 10 wt%, preferably 0.2 to 5 wt%, and wt% represents the amount of metal (calculated in elements) relative to the total weight of the catalyst.

Preferred supports for such palladium and / or platinum containing catalysts are amorphous silica-alumina, more preferably silica-alumina containing 2 to 75 wt% of alumina. Examples of preferred silica-alumina carriers are disclosed in WO-A-9410263. Preferred catalysts include alloys of palladium and platinum, which preferably support C-624, C-654 amorphous silica-alumina carriers from Cryterion Catalyst Company (Houston, TX) as examples of commercially available catalysts.

In step (f), the diesel fuel comprising at least two base oil grades and optionally fractions is separated from the light base oil precursor fraction from step (d) and the hydrogenated oil from step (e). Optional light oils, including base oils and fractions, are preferably separated from the mixture of these streams. This is advantageous because any component present in the heavy base oil precursor fraction that is converted in step (d) to the boiling point range of the light base oil grade contributes to the base oil yield of the light base oil grade.

Since the diesel product obtained as described above undergoes the dewaxing step of the catalyst, a fuel product with very low temperature characteristics and very low amounts of aromatics and sulfur is obtained. In particular, very low sulfur content of less than 10 ppm, low aromatic content of less than 0.1 mmol / 100 g, excellent cooling flow characteristics such as pour point of less than 30 ° C., low temperature filter plugging point of less than 30 ° C., together in step (d) Light oil with is obtained. Diesel oil also has excellent lubrication properties. This in particular mixes light oils such as superior refined blending components with low sulfur light oils. Light oil can also be used as a drilling mud fluid component, electric oil, cutting oil, aluminum rolled oil, fruit spray oil.

Step (f) can be carried out by recovering the product through distillation column operation in near vacuum, as is well known to those skilled in the art. Preferably so-called side strippers are used to separate the base oil product. Intermediate fractions are also recovered to meet the volatility requirements of the desired base oil grade. Preferably, prior to the low pressure distillation step, a high pressure distillation step may be carried out at about atmospheric pressure to separate the gasoline, kerosene, and diesel fractions from the waxed oil individually or into a mixture. This middle distillate fraction is used to obtain a mixture of dewaxed and hydrocracked middle distillate fuel or recycled to step (b). Thus, in step (f) a gaseous supernatant, a liquid supernatant comprising an intermediate distillate, and various base oil grade products such as, for example, spindle oil, light machine oil, heavy machine oil, Obtained from distillation.

In the present invention, the terms used for spindle oil, light machine oil and heavy machine oil may be referred to as base oil grades having kinematic viscosity increasing at 100 ° C., and spindle oil additionally has a maximum volatility specification. The advantage of this process is that it can be achieved for any group of base oils having such different viscosity requirements and volatility specifications. Preferably, the spindle oil is a light base oil product having a kinematic viscosity at 100 ° C. of less than 5.5 cSt, preferably greater than 3.5 cSt. The spindle oil may have a Noack volatility of preferably less than 20% and more preferably less than 18% as determined by the CEC L-40-T87 method, or may have a flash point above 180 ° C. according to ASTM D93. Preferably the hard machine oil has a kinematic viscosity of greater than 6.5 cSt and less than 9 cSt at 100 ° C., more preferably of 8 to 9 cSt. Preferably the heavy machine oil has a kinematic viscosity of greater than 10 cSt and less than 14 cSt at 100 ° C., more preferably 11 to 13 cSt. The corresponding base oil grade may have a viscosity index of 95 to 120. The diesel oil obtained in the process according to the invention can typically be heated to 150-370 ° C. and have a T90 wt% of 340-400 ° C.

The process of the present invention is well illustrated by FIG. 1 shows a hydrocarbon feed line 1 to a hydrocracker 2. The hydrocracked product 3 is separated in the distillation column 4 into gasoline 5, kerosene 6, diesel oil 7, and bottom fraction 8. The bottom fraction or the full range residue 4 is separated into a light base oil precursor fraction 10 and a heavy base oil precursor fraction 11 in a distillation column 9. The light base oil precursor fraction 10 is dewaxed in a dewaxing reactor 12 that produces dewaxed oil (16; second dewaxed oil). The heavy base oil precursor fraction 11 is dewaxed in the dewaxing reactor 13. The dewaxed oil 15 (first dewaxed oil) is hydrotreated in a hydrotreating reactor 14 which produces dewaxed and hydrotreated oil 17. The oils 16 and 17 are mixed. Hydrogen 19 is separated in separator 18 and recycled to dewaxing units 12, 13 after fresh hydrogen 20 is added. The oil 21 is then separated in the distillation column 22 into a low boiling point fraction 26, spindle oil grade 23, light machine oil grade 24, and heavy machine oil 25. The fraction 26 is recycled to the work-up section of the hydrocracker 2 to separate the useful fuel fraction.

Claims (10)

A process for simultaneously providing two or more base oil grades and heavy distillates from deasphalted oil or vacuum distillate feedstock or mixtures thereof, (a) hydrocracking the feedstock to obtain emissions; (b) distilling the effluent obtained in step (a) into a boiling residue and at least one heavy distillate substantially above 340 ° C., (c) separating the residue into a light base oil precursor fraction and a heavy base oil precursor fraction by a subsequent distillation step, (d) lowering the pour point of each base oil precursor fraction separated in the dewaxing reactor of the catalyst operated at the same time and in parallel to obtain a first dewaxed oil and a second dewaxed oil, (e) hydroprocessing the first dewaxed oil obtained by dewaxing the heavy base oil precursor fraction in step (d), (f) separating at least two base oil grades from the second dewaxed oil, the light base oil precursor fraction from step (d) and the hydrogenated oil from step (e), at least two base oil grades and heavy Process for Providing Distillate. The process of claim 1, wherein at least 80 wt% of the residue obtained in step (b) is boiled at 340 ° C. or higher and based on the mixed first and second dewaxing oils in step (d), 400. A process for providing two or more base oil grades and heavy distillates characterized in that between 10 and 40 wt% of the heavy diesel fuel boiling below < RTI ID = 0.0 > 3. The method according to claim 1, wherein 20 to 40 wt% of the heavy base oil precursor fraction obtained in step (c) is recycled to step (a). fair. 4. The two or more base oil grades and heavy distillates according to claim 1, wherein the 10 wt% recovery point of the heavy base oil precursor fraction obtained in step (c) is from 420 to 550 ° C. 5. Process for doing. 5. Process according to claim 4, characterized in that the 10 wt% recovery point of the heavy base oil precursor fraction obtained in step (c) is between 440 and 520 ° C. The process according to any one of claims 1 to 5, wherein the feedstock to step (d) is obtained in a Fischer-Tropsch process and also boils in the boiling range of the heavy base oil precursor fraction and / or the light base oil precursor fraction. At least two base oil grade and heavy distillate, characterized in that it comprises partially isomerized paraffin wax. 7. The process of any of claims 1 to 6, wherein the weight time space velocity in the dewaxing step (d) of the catalyst when treating said light base oil precursor fraction is when treating said heavy base oil precursor fraction. A process for providing at least two base oil grades and heavy distillates characterized by higher than the weight time rate (WHSV) in the dewaxing step (d) of the catalyst. 8. The method of claim 7, wherein said weight time space velocity (WHSV) when processing light base oil precursor fractions is between 1 and 5 kg / l / hr. fair. 9. The pressure according to any one of claims 1 to 8, wherein the pressure at which the light base oil precursor fraction is dewaxed in step (d) is 15 to 65 bars and the pressure at which the heavy base oil precursor fraction is dewaxed. A process for providing at least two base oil grades and heavy distillates, characterized in that it is 250 bars. 10. The process according to any one of claims 1 to 9, wherein step (f) comprises the second dewaxing oil obtained when treating the light base oil precursor fraction and the hydrotreated agent obtained when treating the heavy base oil precursor fraction. 1 Process for providing at least two base oil grades and heavy distillates characterized in that they are carried out in a mixture of dewaxing oil.

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