JP2007515536A - Method for producing cloudy base oil - Google Patents

Abstract

(A) a step in which Fischer-Tropsch wax raw material is contacted with a hydroisomerization catalyst under hydroisomerization conditions at a remote location to reduce the wax content of the raw material, (b) obtained in step (b) Transporting the intermediate product with reduced wax content from one area to another, and (c) solvent dewaxing the transported intermediate product to obtain a non-cloudy base oil near the end user A process for producing a non-cloudy base oil having a kinematic viscosity at 100 ° C. higher than 10 cSt from a Fischer-Tropsch wax feed.
[Selection figure] None

Description

  The present invention relates to a method for producing a base oil having a kinematic viscosity at 100 ° C. higher than 10 cSt.

  Methods for converting gaseous hydrocarbonaceous feedstocks such as methane, natural gas and / or associated gas to liquid products, particularly methanol and liquid or solid hydrocarbons, especially paraffinic hydrocarbons, are described in many references. It is a known method. In this context, it refers to remote areas (eg sand, rainforest) and / or offshore areas where gas is not directly available, usually because there is no large population and / or no industry. There are many. For example, transporting gas in the form of pipelines or liquefied natural gas requires very expensive funding but is not practical.

  On-site Fischer-Tropsch method has been established to efficiently use such standard gas hold. Such methods include a synthesis gas production process using natural gas as a feedstock and a Fischer-Tropsch synthesis process to make heavy wax. WO-A-02070627 describes a method for producing a base oil having a kinematic viscosity of 22 cSt at 100 ° C. from heavy Fischer-Tropsch wax.

The problem with the conventional method is that high viscosity base oils are often cloudy. Such haze makes this method less suitable for use in some applications. However, it is not necessary that all applications of this type of base oil be cloudy.
WO-A-02070627 EP-A-0303622 EP-A-776959 EP-A-668342 US-A-4943672 US-A-5059299 WO-A-9934917 WO-A-9207720 AU-A-698392 WO-A-0014179 EP-A-532118 US-A-4859311 WO-A-9718278 US-A-4343692 US-A-5053373 US-A-5252527 US-A-20040065581 US-A-45744033 EP-A-1029029 US-A-5157191 WO-A-0029511 EP-B-832171 WO-A-0157166 WO-A-9721788 WO-A-0015736 WO-A-0014188 WO-A-0014187 WO-A-0014183 WO-A-0014179 WO-A-0008115 WO-A-9941332 WO-A-0118156 Lubricant Base Oil and Wax Processing, Avilino Sequeira, Jr., Marcel Decker Inc. , New York, 1994, Chapter 7. Lubricant Base Oil and Wax Processing, Avilino Sequeira, Jr., Marcel Decker Inc. , New York, 1994, p162-165.

  The object of the present invention is a process for producing a cloudy base oil in an efficient manner.

The following method achieves this goal.
(A) A step obtained by contacting a Fischer-Tropsch wax raw material with a hydroisomerization catalyst at a remote location under hydroisomerization conditions to reduce the wax content of the raw material (b) The wax obtained in step (a) Transporting the intermediate product with reduced content from one area to another, and (c) dewaxing the transported intermediate product to obtain a non-cloudy base oil at a location close to the end user. ,
A method for producing a non-cloudy base oil having a kinematic viscosity at 100 ° C. higher than 10 cSt from a Fischer-Tropsch wax raw material.

  The method of the present invention is advantageous because step (a) is usually performed remotely. Thus, any low-boiling byproduct can be blended with a remote Fischer-Tropsch low-boiling product. Examples of such products are low viscosity base oils and gas oils. A further advantage of the present invention is that step (c) can be performed in an area closer to the end user. This allows the user of the method to select the dewaxing technique that is most suitable for the particular application. Therefore, if a non-fogging lubricating oil is required, the solvent dewaxing process of the present invention is applied. In contrast, dewaxing techniques with low selectivity can be used if haze is not a major problem. Therefore, it is not necessary to have two types of dewaxing technology at a remote location, and it can be optimally used with existing facilities at a remote location closer to the end user. Another advantage is that all intermediate products can be used efficiently. Since step (c) is a solvent dewaxing step, an oil and high value microcrystalline wax having the desired viscosity characteristics are obtained. Thus, all intermediate products can be sold as products. On the other hand, if the intermediate product is subjected to catalytic dewaxing, a low-boiling by-product having a blend value in a remote area close to the consumer can be obtained. This value is closer to the value of these by-products when dewaxing in remote locations. Another advantage is that there is no need to transport a high quality product such as a non-cloudy base oil or wax produced in step (c) from a remote location to the end user.

  A further advantage is that the wax feed used in step (a) may also contain the heaviest molecules as produced by Fischer-Tropsch synthesis. This produces a high viscosity grade base oil now without the need for deep-cut distillation to remove potential cloudy precursors, as described for example in WO-A-03033622. This is advantageous.

  The Fischer-Tropsch wax used in step (a) is obtained by well-known methods, for example, the Shell Middle Distillate Process (shell intermediate distillation method) or the ExxonMobil “AGC-21” method, so-called Sasol method. These and other methods are described in detail, for example, in EP-A-776959, EP-A-668342, US-A-4943672, US-A-5059299, WO-A-9934917, WO-A-9990720. Yes. The process generally includes a Fischer-Tropsch synthesis and the hydroisomerization steps described in these references.

  More preferably, the wax used in step (a) is produced by the following method. In this method, the Fischer-Tropsch product is subjected to a hydroisomerization step, and a fraction-containing wax is isolated from the product of the hydroisomerization step. More preferably, this fraction is a distillation residue containing the highest molecular weight compounds still present in the product of the hydroisomerization process. The 10 wt% recovery boiling point of this fraction is preferably above 370 ° C, more preferably above 400 ° C, and most preferably above 500 ° C in the specific practice of the invention. When the 10% recovery boiling point of the raw material in step (a) exceeds 500 ° C., the wax content is preferably more than 50% by weight. The raw material of the hydroisomerization step is preferably a Fischer-Tropsch product having 30% by weight or more, preferably 50% by weight or more, more preferably 55% by weight or more of a compound having 30 or more carbon atoms. Further, the weight ratio of the compound having 60 or more carbon atoms and the compound having 30 or more carbon atoms in the Fischer-Tropsch product is at least 0.2, preferably at least 0.4, more preferably at least 0.55. It is. The Fischer-Tropsch product has an ASF-α value (Anderson-Schulz-Flory chain growth factor) of at least 0.925, preferably at least 0.935, more preferably at least 0.945, and even more preferably at least 0.955. It is preferable to derive from the C20 + fraction of

  The initial boiling point of the Fischer-Tropsch product may be in the range of 400 ° C. or less, but is preferably less than 200 ° C. At least a compound having 4 or less carbon atoms and a compound having a boiling point within the range are preferably separated from this synthesis product before being used in the hydroisomerization step.

  Such Fischer-Tropsch products can be obtained by any method that produces a relatively heavy Fischer-Tropsch product. Not all Fischer-Tropsch processes produce such heavy products. An example of a suitable Fischer-Tropsch method is described in WO-A-9934917 and AU-A-698392. These methods can produce a Fischer-Tropsch product as described above.

  Fischer-Tropsch products contain little or no sulfur and nitrogen containing compounds. This is normal for products from the Fischer-Tropsch reaction using synthesis gas containing almost no impurities. Sulfur and nitrogen levels are generally currently below the detection limit of 5 ppm for sulfur and 1 ppm for nitrogen.

  The hydrocracking / hydroisomerization reaction of hydroisomerization is preferably performed in the presence of hydrogen and a catalyst. The catalyst can be selected from those known to those skilled in the art suitable for this reaction. Catalysts for hydroisomerization usually have an acidic functionality and a hydrogenation / dehydrogenation functionality. A preferred acidic functionality is a refractory metal oxide support. Suitable carrier materials include silica, alumina, silica-alumina, zirconia, titania and mixtures thereof. Preferred support materials included in the catalyst used in the process of the present invention are silica, alumina and silica-alumina. A particularly preferred catalyst is one in which platinum is supported on a silica-alumina support. Preferably, if a catalyst containing a halogen compound such as fluorine is used, the catalyst requires special operating conditions and causes environmental problems. Suitable hydrocracking / hydroisomerization processes and suitable catalysts are described in WO-A-0014179, EP-A-532118 and the aforementioned EP-A-776959.

  Preferred hydrogenation / dehydrogenation functionalities are Group VIII metals such as cobalt, nickel, palladium and platinum, more preferably platinum. In the case of platinum and palladium, the catalyst may contain a hydrogenation / dehydrogenation active component in an amount of 0.005 to 5 parts by weight, preferably 0.02 to 2 parts by weight per 100 parts by weight of the support material. When nickel is used, nickel is present in high content and is optionally used with copper. A particularly preferred catalyst used in the hydroconversion stage contains platinum in an amount of 0.05 to 2 parts by weight, more preferably 0.1 to 1 part by weight per 100 parts by weight of support material. In order to increase the strength of the catalyst, the catalyst may also contain a binder. The binder may be non-acidic. Examples are clays and other binders known to those skilled in the art.

In hydroisomerization, the raw material is brought into contact with hydrogen in the presence of a catalyst under high temperature and pressure. The temperature is usually in the range of 175 to 380 ° C, preferably higher than 250 ° C, more preferably 300 to 370 ° C. The pressure is usually in the range from 10 to 250 bar, preferably from 20 to 80 bar. Hydrogen may be supplied at a gas hourly space velocity of 100-10000 Nl / l / hr, preferably 500-5000 Nl / l / hr. The hydrocarbon feed may be fed at an hourly space velocity of 0.1 to 5 kg / l / hr, preferably more than 0.5 kg / l / hr, more preferably less than 2 kg / l / hr. The ratio of hydrogen to hydrocarbon feedstock can range from 100 to 5000 Nl / kg, preferably 250 to 2500 Nl / kg.
The conversion in hydroisomerization, defined as the weight percent with which a feed having a boiling point higher than 370 ° C. per pass reacts to a fraction having a boiling point lower than 370 ° C. is at least 20% by weight, preferably at least 25%. Although it is weight%, Preferably it is 80 weight% or less, More preferably, it is 70 weight% or less. The feedstocks used in the above definition are all hydrocarbon feedstocks supplied to hydroisomerization and therefore include any feedstock that is optionally recycled to step (a).

  In order to obtain at least one middle distillate fuel fraction and wax used in step (a), one or more distillates are separated from the hydroisomerization step effluent. This effluent is preferably subjected to atmospheric distillation. In certain preferred embodiments, the residue obtained by such distillation may be further distilled under conditions close to vacuum to obtain a fraction having a high 10 wt.% Recovery boiling point. Thus, the 10 wt% recovery boiling point of the residue may vary preferably in the range of 350-550 ° C. The atmospheric pressure bottom product or residue preferably has a boiling point exceeding 370 ° C. and is 95% by weight or more. This fraction may be used directly in step (a), or may be subjected to additional vacuum distillation, preferably at a pressure of 0.001 to 0.1 rose. The heavy wax for step (a) is preferably obtained as the bottom product of such vacuum distillation.

  Step (a) may be performed using any hydroconversion process that can reduce the wax content to less than 50% by weight. The wax content of this intermediate product is preferably less than 35% by weight, more preferably 5 to 35% by weight, even more preferably 10 to 35% by weight. A minimum amount of wax is required to perform solvent dewaxing in an optimal manner. The freezing point of the intermediate product obtained in step (a) is preferably less than 80 ° C, more preferably 20 to 60 ° C. The portion of the intermediate product, preferably greater than 50% by weight, more preferably greater than 70% by weight, has a boiling point higher than the 10% by weight recovery point of the wax feed used in step (a). The wax content described here is measured according to the following method. 1 part by weight of the oil fraction to be measured is diluted with 4 parts of a mixture of methyl ethyl ketone and toluene (50/50 volume / volume) and then cooled to −20 ° C. in a freezer. The mixture is subsequently filtered at −20 ° C. The wax is thoroughly washed with a cold solvent, removed from the filter, dried, and weighed. About oil content, the weight% value which deducted wax content (weight%) from 100 weight% is meant.

  A possible method is the hydroisomerization method as described above. It has been found that such a catalyst can be used to reduce the wax to the desired level. The operating conditions necessary to obtain the desired wax conversion can be readily determined by changing the stringency of the process conditions as described above. However, the oil yield is optimized by optimizing a temperature of 300 to 330 ° C. and an hourly space velocity of oil weight of 0.1 to 5 kg / catalyst 1 liter / hour (kg / l / hr), more preferably 0.1 ˜3 kg / l / hr is particularly preferred.

  A more preferred type of catalyst that can be applied to step (a) is a dewaxing catalyst system. The process conditions applied when using this type of catalyst must be such that the wax content remains in the oil. In contrast, conventional catalytic dewaxing methods aim to reduce the wax content to almost zero. With a dewaxing catalyst containing molecular sieves, many of the heavy molecules will remain in the dewaxed oil. Therefore, in this case, a more viscous base oil is obtained.

  The dewaxing catalyst applicable to step (a) preferably contains a combination of molecular sieves and optionally a metal having a hydrogenating function such as a Group VIII metal. Molecular sieves, more preferably molecular sieves having a pore diameter of 0.35 to 0.8 nm, showed good catalytic ability for reducing the wax content of the wax feed. Suitable zeolites are mordenite, ZSM-5, ZSM-12, ZSM-22, ZSM-23, SSZ-32, ZSM-35 and ZSM-48, or combinations of these zeolites. Another preferred molecular sieve group is the silica-alumina phosphate (SAPO) material, of which SAPO-11 is most preferred, as described, for example, in US-A-4859311. ZSM-5 may optionally be used in the form of HZSM-5 in the absence of a Group VIII metal. Other molecular sieves are preferably used in combination with Group VIII metals. Preferred Group VIII metals are nickel, cobalt, platinum and palladium. Examples of possible combinations are Pt / ZSM-35, Ni / ZSM-5, Pt / ZSM-23, Pd / ZSM-23, Pt / ZSM-48 and Pt / SAPO-11, or Pt / Zeolite β and Pt / ZSM-23, Pt / Zeolite β and Pt / ZSM-48 or Pt / Zeolite β and Pt / ZSM-22 stacked structure. Further details and examples of suitable molecular sieves and dewaxing conditions are described, for example, in WO-A-9718278, US-A-4434369, US-A-5053373, US-A-5252527, US-A-20040065581, US-A. -4574043 and EP-A-1029029.

  A preferred type of molecular sieve is a molecular sieve with relatively low isomerization selectivity and high wax conversion selectivity, such as ZSM-5 and ferrierite (ZSM-35).

  The dewaxing catalyst preferably also contains a binder. The binder may be a synthetic or naturally occurring (inorganic) material such as clay, silica, and / or metal oxide. Naturally occurring clays are, for example, montmorillonite and kaolin. The binder is preferably a porous binder material such as refractory oxides such as alumina, silica-alumina, silica-magnesia, silica-zirconia, silica-tria (thorium oxide), silica-berylria (beryllium oxide), silica-titania, There are ternary compositions such as silica-alumina-tria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia. It is further preferred to use a low acidity refractory oxide binder material that is essentially free of alumina. Examples of these binder materials include silica, zirconia, titanium dioxide, germanium dioxide, boria and mixtures of two or more of these as described above. The most preferred binder is silica.

  A preferred type of dewaxing catalyst comprises intermediate zeolite crystallites as described above and a low acidity refractory oxide essentially free of alumina. The surface of this aluminosilicate zeolite microcrystal is modified by surface dealumination treatment. A preferred dealumination treatment is by contacting the binder and zeolite extrudates with an aqueous solution of a fluorosilicate salt as described, for example, in US-A-5157191 or WO-A-0029511. Examples of suitable dewaxing catalysts as described above are silica-bonded dealumina Pt / ZSM-5, silica-bonded dealumina Pt / ZSM-35 as described, for example, in WO-A-0029511 and EP-B-832171. It is.

  The conditions for step (a) when using a dewaxing catalyst are usually 200-500 ° C., suitably 250-400 ° C., preferably 300-330 ° C., operating temperature 10-200 bar, preferably 40 Hydrogen pressure in the range of ~ 70 bar, 0.1 to 10 kg of oil per liter of catalyst per hour (kg / l / hr), preferably 0.1 to 5 kg / l / hr, more preferably 0.1 Includes hourly space velocities (WHSV) in the weight range of ˜3 kg / l / hr, and hydrogen to oil ratios in the range of 100 to 2,000 liters of hydrogen per liter of oil.

  The transportation in the step (b) is preferably carried out by ship. The location where step (a) is performed is preferably a remote location, and the location where step (c) is performed is preferably closer to the end user of the base oil. When the product is loaded into the ship's product container, it is preferred to first purge the ship's empty product container with nitrogen in order to reduce the oxygen content. This purge is preferably performed for 5 minutes or more, more preferably for 10 minutes or more. After purging, the product container is loaded with the intermediate product. Preferably, nitrogen is supplied to the loaded container so that the gas space above the product in the product container has a nitrogen atmosphere. More preferably, nitrogen is supplied to the loaded container for 5 minutes or more, more preferably for 10 minutes or more. The transport period of step (b) usually exceeds 5 days. The nitrogen used is preferably such that it is obtained when oxygen is isolated from air in an air separation unit. This oxygen is typically used in the production of synthesis gas, which is then used to make FT wax as a feedstock for the Fischer-Tropsch reaction.

In step (c), the intermediate product carried in step (b) is solvent dewaxed to obtain a cloudless oil. Solvent dewaxing is well known to those skilled in the art, and the step of mixing one or more solvents and / or wax precipitants with the base oil precursor fraction, the mixture in the range -10 ° C to -40 ° C, preferably -20 ° C Cooling to a temperature in the range of −35 ° C. to separate the wax from the oil. The wax-containing oil is typically filtered through a filter cloth, such as a textile fiber cloth, such as cotton, a porous metal cloth, or a synthetic cloth cloth. Examples of solvents that can be used in the solvent dewaxing process include C ₃ -C ₆ ketones (eg, methyl ethyl ketone, methyl isobutyl ketone and mixtures thereof), C ₆ -C ₁₀ aromatic hydrocarbons (eg, toluene), ketones and aromatics, mixture (such as methyl ethyl ketone and toluene), a self-refrigerating properties (Autorefrigerative) solvent, such as propane, Purobiren, butane, normally gaseous liquefied _C 2 -C ₄ hydrocarbons such as butylene, and mixtures thereof. In general, a mixture of methyl ethyl ketone and toluene or methyl ethyl ketone and methyl isobutyl ketone is preferred. These and other suitable examples are described in Lubricant Base Oil and Wax Processing, Avilino Sequeira, Jr, Marcel Decker Inc. , New York, 1994, Chapter 7.

In step (c) wax is also obtained. Such waxes have been found to be relatively soft microcrystalline waxes that can be used for various purposes. Another advantage of the present invention is that wax is recovered from the intermediate product at a location close to the end consumer. The freezing point of the microcrystalline wax obtained by the above method is preferably 85 to 120 ° C., more preferably 95 to 120 ° C. as measured by ASTM D938, and PEN at 43 ° C. is measured by IP 376. , Exceeding 0.8 mm, preferably exceeding 1 mm. The wax is further characterized by containing less than 1% by weight of aromatic compounds and less than 10% by weight of naphthenic compounds, more preferably less than 5% by weight. Branched olefins in the _wax, as determined by C 13 NMR, preferably more than 33 mol%, more preferably above 45 mol%, also less than 80 mol%. This method measures the average molecular weight of the wax, followed by the mole% of molecules with methyl branches, the mole% of molecules with ethyl branches, the mole% of molecules with C ₃ branches, and the molecules with C ₄ + branches. Measure mol%. However, each molecule is assumed to have no more than two branches. The mol% of these branched paraffins is the sum of the mol% of each branched paraffin. In this way, the mole% of average molecules in the wax with only one branch was calculated. In practice, paraffin molecules with more than one branch may exist. Therefore, the content of branched paraffin calculated by other methods may show different values.

  The oil content of the wax is usually less than 10% by weight, more preferably less than 6% by weight, as measured by ASTM D721. If a low oil content is desired, it may be advantageous to perform a separate deoiling step. Deoiling methods are well known and are described, for example, in Lubricant Base Oil and Wax Processing, Avilino Sequeira, Jr, Marcel Decker Inc. , New York, 1994, p162-165. The oil content of the wax after deoiling is preferably 0.1 to 2% by weight. The lower limit is not important. Values above 0.5% by weight can be expected, but lower values can be achieved according to the method of obtaining the wax. The most likely oil content is 1-2% by weight. The kinematic viscosity at 150 ° C. of the wax is preferably greater than 8 cSt, more preferably greater than 12 cSt and less than 18 cSt.

  The kinematic viscosity of a non-cloudy base oil at 100 ° C. is preferably greater than 10 cSt, more preferably greater than 14 cSt, and this viscosity may range up to 30 cSt or more. The pour point is preferably less than -5 ° C, more preferably less than -18 ° C, and even more preferably less than -21 ° C. The viscosity index is suitably above 120, preferably above 130. Non-cloudy base oil is measured at the cloud point. The cloud point of a non-cloudy base oil according to the present invention is close to the pour point and less than 0 ° C, preferably less than -10 ° C, more preferably less than -15 ° C, as measured by ASTM D2500.

  From these properties, Applicants have found that they can be advantageously used in the manufacture of lubricating oil compositions that do not require a viscosity modifier (VM). Applicants have further found that lubricating oils without viscosity modifiers can be obtained without the need to add poly alpha-olefin co-base oils as shown in WO-A-0157166. Accordingly, the present invention preferably blends a Fischer-Tropsch derived low viscosity base oil with the cloudless base oil obtained in step (c) and one or more additives to provide a VM-free lubricating oil composition. It is also directed to a method of manufacturing a product. The low viscosity base oil has a kinematic viscosity at 100 ° C. of less than 7 cSt. The kinematic viscosity at 100 ° C. of a non-cloudy base oil is preferably greater than 10 cSt, more preferably greater than 14 cSt, most preferably greater than 18 cSt.

  Applicants have found that blending a non-cloudy base oil with a low viscosity grade base oil provides the properties of a so-called SAE “xW-y” viscosity lubricant formulation without the need to add a viscosity modifier. It was. Furthermore, applicants have found that when a lubricant that does not contain a viscosity modifier is used as an automotive engine lubricant in a gasoline direct injection (GDI) engine, residue build-up occurs behind the inlet valve tulip (if VM exists) I found it never happened.

  In addition, it has been found that lubricating oil formulations with a SAE “xW-y” (yx = 25 or more) viscosity can be produced without the need to add VM. According to the teaching of WO-A-0157166, it is expected that such a formulation can only be produced with the addition of VM.

The pour point of a low viscosity Fischer-Tropsch derived base oil having a kinematic viscosity at 100 ° C. of less than 7 cSt is preferably less than −18 ° C., more preferably less than −27 ° C. The kinematic viscosity at 100 ° C. is preferably more than 3.5 cSt, more preferably 3.5 to 6 cSt. The viscosity index (VI) is preferably greater than 120, more preferably greater than 130. VI is typically less than 160. The Noack volatilization loss (according to CEC L40 T87) is preferably less than 14% by weight. The low viscosity component is a normal API group III base oil, more preferably, for example, EP-A-776959, EP-A-668342, WO-A-97272188, WO-A-0015736, WO-A-0014188, WO -A-0014187, WO-A-0014183, WO-A-0014179, WO-A-0008115, WO-A-9941332, EP-A-1029029, WO-A-0118156 and WO-A-0157166 Such as Fischer-Tropsch derived base oil.
The invention is illustrated by the following non-limiting examples.

Example 1
A distillation residue having the properties shown in Table 1 was isolated from hydroisomerized Fischer-Tropsch wax. The wax content measured after solvent dewaxing at a dewaxing temperature of −20 ° C. was 34.1% by weight.

  The residue was contacted with a catalyst consisting of 0.7 wt% platinum, 25 wt% ZSM-12, and a silica binder. The dewaxing conditions are a hydrogen pressure of 40 bar, WHSV = 1 kg / l · h, and a hydrogen speed of 500 Nl / kg of raw material. This experiment was performed at three different temperatures. See Table 2 for results.

  The fractions with boiling points exceeding 485 ° C. obtained in 1a, 1b and 1c were easy to transport. The fraction to be transported can optionally also contain a liquid fraction with a boiling point below 485 ° C. obtained in the catalytic dewaxing step. The transportable intermediate product was then solvent dewaxed with a mixture of methyl ethyl ketone and toluene (50/50 vol / vol) solvent at a dewaxing temperature of -20 ° C. The properties and yield of the oil obtained are shown in Table 3.

  FIG. 1 was created based on the experimental results. From FIG. 1, it can be seen that increasing the catalytic dewaxing stringency decreases the yield of 485 ° C. + fraction and the yield after solvent dewaxing passes through the maximum.

Example 2
A distillation residue having the properties shown in Table 4 was isolated from hydroisomerized Fischer-Tropsch wax. The wax content measured after solvent dewaxing at a dewaxing temperature of −20 ° C. was 41% by weight.

  The residue was contacted with a catalyst consisting of 0.7 wt% platinum, 25 wt% ZSM-12, and a silica binder. The dewaxing conditions are a hydrogen pressure of 40 bar, WHSV = 1 kg / l · h, and a hydrogen speed of 500 Nl / kg of raw material. This experiment was conducted at 340 ° C. From the partially dewaxed oil, compounds having a boiling point of less than 500 ° C. were removed by distillation. The remaining fraction containing 34% by weight of wax was a liquid slurry at room temperature and was easy to transport. See also the results in Table 5.

  Liquid slurry fractions with boiling points above 500 ° C. were solvent dewaxed using a mixed (50/50 vol / vol) solvent of methyl ethyl ketone and toluene at a dewaxing temperature of −20 ° C. The properties and yield of the oil obtained are shown in Table 6.

The yield change by the dewaxing temperature of the fraction exceeding the boiling point 485 degreeC of 3 types in Example 1 is shown.

Claims (12)

(A) contacting a Fischer-Tropsch wax feedstock with a hydroisomerization catalyst at a remote location under hydroisomerization conditions to reduce the wax content of the feedstock;
(B) transporting the intermediate product with reduced wax content obtained in step (a) from one area to another, and (c) solvent dewaxing the transported intermediate product to the end user Obtaining a non-cloudy base oil at a location close to
A method for producing a non-cloudy base oil having a kinematic viscosity at 100 ° C. higher than 10 cSt from a Fischer-Tropsch wax raw material.   The process according to claim 1, wherein the raw material of step (a) has a 10% by weight boiling point higher than 500 ° C and a wax content higher than 50% by weight.   The method according to claim 2, wherein the wax content in the raw material is 60 to 95% by weight.   The method according to claim 2 or 3, wherein a 10% by weight recovery boiling point of the raw material is 500 to 550 ° C.   The process according to any one of claims 1 to 4, wherein the wax content in the intermediate product is 10 to 35% by weight.   The method according to any one of claims 1 to 5, wherein the freezing point of the intermediate product is 20 to 60 ° C.   The process according to any one of claims 1 to 6, wherein the boiling point of the intermediate product exceeding 50% by weight is higher than the 10% by weight recovery boiling point of the raw material used in step (a).   The process according to claim 7, wherein the boiling point of the intermediate product exceeding 70% by weight is higher than the 10% by weight recovery boiling point of the raw material used in step (a).   9. The hydroisomerization catalyst used in step (a) is a substantially amorphous catalyst comprising a silica-alumina support and a Group VIII noble or non-noble metal, according to any one of claims 1-8. Method.   The process according to claim 8, wherein the hydroisomerization catalyst used in step (a) is a molecular sieve-based catalyst and a substantially amorphous catalyst comprising a Group VIII noble or non-noble metal.   Step (b) is carried out on the ship, the ship's container is first purged with nitrogen before loading, this nitrogen is obtained in an air separation unit, which also isolates oxygen to produce syngas, and then this 11. A process according to any one of the preceding claims, wherein synthesis gas is used as a feedstock for Fischer-Tropsch wax production.   Viscosity adjustment characterized by blending a low-viscosity base oil with the cloudless base oil obtained in step (c) of the process according to any one of claims 1 to 11 and one or more additives. A method for producing a lubricating oil composition containing no additive.