Isomerisation process using metal-modified fine-crystalline mtt molecular sieve

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing base oil which involves bringing C10+ hydrocarbon material into contact with a catalyst and hydrogen in isomerisation conditions to obtain base oil. The catalyst contains a molecular sieve, having the topology of a MTT structure and crystallite diameter from 200 to 400 Å in the longest direction, at least one metal selected from a group consisting of Ca, Cr, Mg, La, Na, Pr, Sr, K and Nd, and at least one group VIII metal. The invention also relates to versions of a method for deparaffination of hydrocarbon material, using a similar catalyst.

EFFECT: use of the present invention enables to obtain a product with improved viscosity index at lower flow temperatures.

30 cl, 6 ex, 3 tbl, 11 dwg

 

The technical FIELD TO WHICH the INVENTION RELATES.

The present invention relates to a method of isomerization of raw materials, which includes a linear chain and slightly branched paraffins containing 10 or more carbon atoms using a catalyst comprising crystalline MMT molecular sieve, rich in metals. The present invention also relates to methods of dewaxing to obtain products with improved viscosity indices at lower temperatures yield.

PRIOR art

The production of base oils, group II and group III with the use of hydrogenation in recent years has become increasingly important. Constantly work on finding catalysts that exhibit high selectivity to isomerization and conversion. As discussed in U.S. patent No. 5282958, column 1-2, well aware of the use of molecular sieves with an intermediate pore size, such as ZSM-22, ZSM-23, ZSM-35, SSZ-32, SAPO-11, SAPO-31, SM-3, SM-6, for isomerization and dewaxing, selective to the form. Other typical zeolites used in the dewaxing include ZSM-48, ZSM-57, SSZ-20, EU-1, EU-13, Ferrera, SUZ-4, theta-1, NU-10, NU-23, NU-87, ISI-1, ISI-4, KZ-1 and KZ-2.

U.S. patents 5252527 and 5053373 describe such a zeolite, as SSZ-32, which is obtained using cation N-lower alkyl-N'-isopropylene saline, as a sample. Patent 5053373 suggests using the ratio of silica to alumina from more than 20 to less than 40 index and permeability after annealing and gidrirovannoe form 13 or more. The zeolite in the patent 5252527 not limited to the index of the permeability of 13 or more. In the patent 5252527 asked to fill zeolites metals in order to provide the functions of the hydrogenation-dehydrogenization. Typical cations substitution can include a hydrogen atom, ammonium, cations of metals such as rare earth metals of group IIA and group VIII, and mixtures thereof. The method of obtaining zeolites MTT type, such as SSZ-32 and ZSM-23, using small, neutral amines proposed in U.S. patent No. 5707601.

U.S. patent No. 5397454 reveals how hydroconversion involving the use of zeolite as SSZ-32, which has the crystallites of small size and the index of the permeability of 13 or more after calcination and in gidrirovannoe form. The catalyst has a ratio of silicon oxide to aluminum oxide greater than 20 and less than 40. U.S. patent No. 5300210 also relates to methods for the conversion of hydrocarbons with the use of SSZ-32. SSZ-32 of U.S. patent No. 5300210 is not limited to the crystallites of small size.

U.S. patent No. 7141529 discloses the modification of molecular sieves of various metals (metal or metal is om, selected from the group comprising Ca, Cr, Mg, La, Ba, Pr, Sr, K and Nd, as well as metals of group VIII) obtaining catalysts with improved selectivity of isomerization using nC16of raw materials. None of the methods can not obtain the molecular sieve with a small crystallite size. None of the methods isomerization does not tilt according to the VI of the product, boiling at 650°F (343°C) and higher temperature fluidity zero or less.

The patent publication U.S. No. 2007/A discloses a method of obtaining a crystalline MTT catalyst. Not proposed modification of metals molecular sieve.

SUMMARY of the INVENTION

A method of dewaxing a hydrocarbon feedstock with getting isomerizing product, raw material includes a linear chain and slightly branched paraffins containing 10 or more carbon atoms, the method includes providing contact between the feedstock in the isomerization conditions in the presence of hydrogen with a catalyst comprising the molecular sieve of the MTT structural topology and containing crystallites with a diameter of from about 200 to about 400 Å in the longest direction, the catalyst contains at least one metal selected from the group comprising Ca, Cr, Mg, La, Na, Pr, Sr, K and Nd, and at least one metal of group VIII.

P is idlogin way dewaxing, including isomerization the dewaxing of hydrocarbons containing at least 5% of the mass. wax, over a catalyst to produce two or more isomerized product, boiling at 343°C (650°F) or above, each isomerized product has

a) the temperature fluidity between 0 and -30°C, and

b) corresponding to the viscosity index of 95 or above;

with direct, the corresponding graph of the temperature dependence of yield strength on the x-axis from viscosity indices on the y-axis has a slope for y zero or less.

Also, a method of dewaxing, including isomerization the dewaxing of hydrocarbons containing at least 5% of the mass. wax, over a catalyst to produce two or more isomerized product, boiling at 343°C (650°F) or above, each isomerized product has

a) the temperature fluidity between 0 and -30°C, and

b) corresponding to the viscosity index of 95 or above;

with direct, the corresponding graph of the temperature dependence of yield strength on the x-axis from viscosity indices on the y-axis has a slope for y zero or less; and the output of the two or more isomerized product, boiling at 343°C (650°F) or above, 80% of the mass. or more per raw.

BRIEF DESCRIPTION of DRAWINGS

Figure 1 shows the output depending on the temperature fluidity for isomer is implementing a heavy neutral raw materials (500N) using a standard MTT-containing catalyst (“Standard SSZ-32”), modified metal standard MTT-containing catalyst ("modified metal SSZ-32") and a modified metal MTT-containing catalyst with small crystallites ("modified metal SSZ-32").

Figure 2 presents the dependence of the viscosity index (VI) temperature fluidity for isomerization of heavy neutral (500N) raw materials using standard MTT-containing catalyst (“standard SSZ-32”), modified metal standard MTT-containing catalyst (“modified metal SSZ-32”) and a modified metal MTT-containing catalyst with small crystallites (“Modified metal SSZ-32X”).

Figure 3 shows the dependence of the yield of gas (formation of C1-C4products) from the temperature fluidity for isomerization of heavy neutral (500N) raw materials using standard MTT-containing catalyst ("standard SSZ-32"), modified metal standard MTT-containing catalyst ("modified metal SSZ-32") and a modified metal MTT-containing catalyst with small crystallites ("modified metal SSZ-32").

Figure 4 shows the dependence of the yield of C8products from temperature fluidity for isomerization of heavy neutral (500N) raw materials using andariego MTT-containing catalyst (“standard SSZ-32”), modified metal standard MTT-containing catalyst (modified metal SSZ-32) and the modified metal MTT-containing catalyst with small crystallites (“modified metal SSZ-32”).

Figure 5 shows the dependence of the yield on temperature fluidity for isomerization 150N raw materials using standard MTT-containing catalyst (standard SSZ-32”), MTT-containing catalyst with a small crystallites without added metal (crystalline SSZ-32”), modified metal standard MTT-containing catalyst (“modified metal SSZ-32”) and a modified metal crystalline MTT-containing catalyst (“modified metal SSZ-32”).

Figure 6 shows the dependence of the viscosity index (VI) temperature fluidity for isomerization 150N raw materials using standard MTT-containing catalyst (standard SSZ-32”), modified metal standard MTT-containing catalyst (“modified metal SSZ-32”) and a modified metal crystalline MTT-containing catalyst (“modified metal SSZ-32”).

7 shows the dependence of the exit gas temperature fluidity for isomerization 150N raw materials using standard MTT-containing catalysis of the Torah (standard SSZ-32”), modified metal standard MTT-containing catalyst (“modified metal SSZ-32”) and crystalline MTT-containing catalyst (“modified metal SSZ-32”).

On Fig shows the dependence of the yield of light products synthetic gasoline (C8-250°F) (8-121,11°C) temperature fluidity for isomerization 150N raw materials using standard MTT-containing catalyst (standard SSZ-32”), modified metal standard MTT-containing catalyst (“modified metal SSZ-32”) and a modified metal crystalline MTT-containing catalyst (“modified metal SSZ-32”).

Figure 9 shows the dependence of the yield on temperature fluidity for isomerization medium-neutral raw materials using standard MTT-containing catalyst (standard SSZ-32”), modified metal standard MTT-containing catalyst (“modified metal SSZ-32”) and a modified metal crystalline MTT-containing catalyst (“modified metal SSZ-32”).

Figure 10 shows the dependence of the viscosity index (VI) temperature fluidity for isomerization medium-neutral raw materials using standard MTT-containing catalyst (standard SSZ-232)option is sale metal standard MTT-containing catalyst (“modified metal SSZ-32”) and a modified metal crystalline MTT-containing catalyst (“modified metal SSZ-32”).

Figure 11 provides a comparison of the x-ray standard MTT molecular sieve (STANDARD SSZ-32") and a crystalline molecular sieve ("SSZ-32").

DETAILED DESCRIPTION of embodiments of the INVENTION

In one embodiment of the invention, the catalyst comprises a molecular sieve having MTT topology. The used catalyst comprises from 5 to 85 wt%. molecular sieves. "Molecular sieve"as used herein, may include "zeolites". The term “zeolite MMT type”, “MTT molecular sieve” or its variation relates to the structural code of the structure of a family of materials molecular sieves. Commission on the structure of the international Association for the zeolite (IZA) provides codes consisting of three letters of the alphabet for zeolites (type molecular sieves), having a structure that is defined. Zeolites having the same topology, in General, called these three letters. Code MTT given the structure of the molecular sieves include ZSM-23, SSZ-32, EU-13, ISI-4, KZ-1. Thus, zeolites having the structure, is the same as that of the ZSM-23 and SSZ-32, referred to as zeolites MTT-type.

Other molecular sieves used for isomerization dewaxing, are molecular sieves with an intermediate pore size, with the topology structure of the MTT, TON, AEL or FER.

Crystalline zeolites MTT t is PA, used in one embodiment of the catalyst, have a diameter of crystallites of approximately 200 Å to approximately 400 Å in the longest direction.

OBTAINING CATALYST

In one embodiment of the invention the crystalline molecular sieve MTT type is obtained from an aqueous solution containing sources of an oxide or hydroxide of alkaline metal, alkylamine (such as isobutylamine), the source of organic carbon compounds Quaternary ammonium ion, which subsequently enters the ion exchange with the formation of hydroxide to form aluminum oxide (for example, where the source of aluminum oxide gives the aluminum oxide, which is covalently distributed on the silicon oxide and silicon oxide. In one embodiment of the invention the source of organic carbon compounds Quaternary ammonium ion, which subsequently enters the ion exchange with the formation of hydroxide form, represents a cation, N-lower alkyl-N'-isopropylimidazole (for example, the cation is N,N'-diisopropylethylamine or cation N-methyl-N'-isopropylimidazole). The aqueous solution has a composition in units of mole fractions falling within the following intervals:

Table 1
The composition in molar fractions
Variant implementation of the invention 1Variant implementation of the invention 2
SiO2/Al2O320 under 4030-35
OH /SiO2of 0.10 to 1.00,20-0,40
Q/SiO20,05-0,500,10-0,25
M+ /SiO20,05-0,300,15-0,30
H2O/SiO220-30025-60
Q/Q+M+0,25-0,750,33-067

where Q represents the sum of Qaand Qb; M denotes an oxide or hydroxide of an alkali metal and M+ denotes a cation of an alkali metal, formed by an oxide or hydroxide of an alkali metal. Alkali metals are a series of elements comprising group I (the system IUPAC) periodic table: lithium (Li), sodium (Na), potassium (K), rubidium (Rb), cesium (Cs), France (Fr).

Qais a Quaternary ammonium ion on the basis of the e organic carbon and Q bis an amine. In one embodiment of the invention Qarepresents a cation, N-lower alkyl-N'-isopropylimidazole (for example, the cation is N,N'-diisopropylethylamine or cation N-methyl-N'-isopropylimidazole). Can be used a number of different amines Qb.In one embodiment of the invention suitable examples Qbare isobutylamine, neopentylene, monoethylamine or mixtures thereof. The molar concentration of Qbmore than the molar concentration of Qa. In General, the molar concentration of Qbis in the range of from 2 to about 9-fold molar concentration of Qa. U.S. patent No. 5785947 (introduced in the text by reference) describes a method of synthesis of the zeolite, involving the use of two organic nitrogen sources, one source, which represents an amine containing from one to eight carbon atoms, provides significant savings compared with a method in which the ion source of Quaternary ammonium (such as imidazole) is the only source of organic component. The combination of the two sources of organic nitrogen gives the possibility of nucleation in the initial matrix (used in a smaller amount) of the desired structure of the zeolite, and then amine, facilitating the filling then roll clicks the zoom during crystal growth. Empty the pores of the zeolites with high silicon dioxide content tend to re-dissolve in the synthesis conditions. Two amine can also help maintain high alkalinity for synthesis.

In one embodiment of the invention, the ion source of the Quaternary ammonium organic carbon also gives a hydroxide ion.

In one embodiment of the invention, the ion source of the Quaternary ammonium organic carbon compounds, Qa, an aqueous solution formed by a compound of the formula

where R represents alkyl containing from 1 to 5 carbon atoms, for example, -CH3or isopropyl. Anion (Θ), that does not harm the education MTT molecular sieve, is associated with a cation. Examples of the anion include halogen (e.g. chloride, bromide and iodide), hydroxide, acetate, sulfate, carboxylate, etc. Hydroxide is particularly suitable for use anion.

The reaction mixture is prepared using standard methods for zeolites. Typical sources of aluminum oxide for the reaction mixture include aluminates, alumina, and aluminum compounds, such as coated aluminum colloids on the basis of silicon dioxide (one example is a colloidal Sol Nalco 1056), Al2(SO4)3 and other zeolites.

In one embodiment of the invention, the aluminum oxide is covalently dispersed form on the silicon dioxide. The aluminum oxide in covalently dispersed form allows you to crystallize the molecular sieve with a high content of aluminum. The high content of aluminum in the molecular sieve accelerates the isomerization. In another approach can be used zeolites with structure Pancasila and lower relationship silicon dioxide/aluminum oxide (about 10) as sources of aluminum oxide or raw materials for the synthesis of small crystal MTT molecular sieves. These zeolites are crystalline to crystalline MTT molecular sieves in the presence of organic sources Qaand Qbabove.

Mordenite and ferrierite zeolites are two data valuable source of aluminum oxide or raw materials. Last zeolites have also been used for the crystallization of ZSM-5 and ZSM-11 (U.S. patent No. 4502024).

Another approach, in which the aluminum oxide is covalently dispersed form on the silicon dioxide based on the use of coated alumina Sol of silicon dioxide, such as produced by Nalco Chem. Co. under the trade name of the colloidal Sol 1056 (26% silica, 4% aluminum oxide). In addition to creating in n the PTO SSZ-32X high aluminum content, the use of Zola promotes the formation of crystallite size of less than 1000 Å (along the major axis) with unexpectedly high isomerization ability.

In one embodiment of the invention the catalytic properties of molecular sieves MTT (gidrirovannoe form) for kekirawa ability is confirmed by the values of the permeability index (as defined in J. Catalysis 67, page 218) 13 or more, and in one embodiment of the invention MTT molecular sieve (gidrirovannoe form) has an index of permeability from 13 to 22. The index definition permeability is also disclosed in U.S. patent No. 4481177. In General, the decrease of the crystallite size of the zeolite leads to lower selectivity on the form. This is shown for reactions of ZSM-5, including aromatic compounds, J. Catalysis 99, 327 (1986). In addition, it was found that zeolite ZSM-22 (U.S. patent No. 4481177) is closely associated with the ZSM-23 (J. Chem. Soc. Chem. Comm. 1985, page 1117). In the above link on ZSM-22 was shown that grinding in a ball mill crystallites leads to the production of the catalyst permeability index of 2.6. This unexpectedly low value for this material was the impetus for conducting other studies that have shown that it is very selective 10-nuclear pentasil (Proc. of 7thIntl. Zeolite Conf. Tokyo, 1986, page 23). Apparently, grinding ball mill leads to education is aniu less selective, but more active catalyst due to the receipt of smaller crystallites. In contrast to the previously known catalysts with small crystallites with low indexes of the permeability of this small crystallite MTT molecular sieve saturated with metals, maintains high selectivity.

Typical sources of silicon oxide include silicates, the hydrogel of silica, silicic acid, colloidal silica, fume silica, tetrachlorozincate and hydroxides of silicon dioxide. Can be added or formed in the reaction medium salts, especially halides of alkali metals, such as sodium chloride. In the literature they are described as contributing to the crystallization of zeolites and at the same time warning occlusion of silicon dioxide in crystal lattice.

The reaction mixture is supported at an elevated temperature until, until crystals are formed molecular sieve. The temperature at the stage of the hydrothermal crystallization is usually supported from about 140°to about 200°C., for example, from about 160°to about 180°C., or from about 170°to about 180°C. the Period of crystallization is typically greater than 1 day, and in one embodiment of the invention the period of crystallization is from about 4 days before when listello 10 days.

Hydrothermal crystallization was carried out under pressure and usually in an autoclave so that the reaction mixture is subject to the effects of autogenic pressure. The reaction mixture can be mixed with the introduction of components, and in the course of crystallization.

Once the molecular sieve crystals have formed, the solid product is separated from the reaction mixture by standard methods of mechanical separation, such as filtration or centrifugation. The crystals are washed with water, and then dried, for example at a temperature from 90°C to 150°C for a time ranging from 8 to 24 hours from the receipt of the molecular sieve crystals after crystallization. Stage drying can be conducted at atmospheric or reduced pressure.

In the process stage hydrothermal crystallization crystals yet to crystallize from the reaction mixture spontaneously. In the reaction mixture can also be introduced seed crystals of MTT crystals, as in a direct and rapid crystallization, and to minimize undesirable aluminosilicate dirt.

In one embodiment of the invention crystalline zeolites MTT type, used as a catalyst, have a diameter of crystallites from approximately 200 Å to approximately 400 Å in the longest direction.

In one var is ante the invention, the crystalline molecular sieve of the MTT can be used after synthesis or can be thermally treated (calcined). The annealing is mainly carried out at a temperature of approximately 750°F (398,89°C). Usually it is desirable to remove the cation of the alkali metal ion exchange resins and to substitute a hydrogen atom, ion ammonium, or any desired metal ion. Molecular sieve can be wimalasena chelat forming agents, for example EDTA or diluted solutions of acids, to increase the molar ratio of silica/alumina. Molecular sieve can also be steamed. Steam treatment helps to stabilize the crystal lattice to the action of acids.

The calcined molecular sieve and then saturate at least one metal selected from the group comprising Ca, Cr, Mg, La, Na, Pr, Sr, K and Nd. These metals are known for their ability to modify the operational characteristics of the catalyst by reducing the number of strong acid centers on the catalyst and reduce the selectivity to kikirowy in favor isomerization. In one embodiment of the invention, the modification also includes the increased distribution of metal, so that acidic or cationic centers in the catalysts are blocked. In one embodiment of the invention the feeding of the metal is carried out by various methods including impregnation and ion exchange. Typically, the saturation met Lom is so, the catalyst contains from 0.5 to 5% of the mass. metal calculated on the dry matter. In one embodiment of the invention, the catalyst contains from 2 to 4% of the mass. metal calculated on the dry matter.

Typical ion exchange techniques include the implementation of contact of the extrudate or granulate with a solution containing a salt of the desired replacing cation or cations. Although it may be used a large number of salts, in one embodiment of the invention the salt of the desired replacing cation or cations selected from the group of chlorides and other halides, nitrates, sulfates and mixtures thereof. Explanatory methods of ion exchange is considered in a large number of patents, including U.S. patent No. 3140249, 3140251 and 3140253, each of which is introduced in the present document by reference. Ion exchange can take place either before or after calcination of the extrudate or granulate. The calcination is carried out in the temperature range from 400 to 1100°F (204,44-593,33°C).

After making contact with a solution of salt of the desired replacing cation, the molecular sieve is dried at temperatures in the range from 149°F (60°C) up to about 599°F (315°C). Molecular sieve and optionally saturated, using a method such as impregnation, the metal of group VIII with increasing hydrogenation steps. In some embodiments, the implementation izobretatelni to carry out simultaneously the joint impregnation of the modifier metal and a metal of group VIII, as proposed in U.S. patent 4094821. In one embodiment of the invention the metal of group VIII is platinum, palladium or a mixture of two metals. In one embodiment of the invention after the saturation of the metal material can be calcined in air or in an atmosphere of inert gas at temperatures from 500 to 900°F (260 to 482,22°C).

Thus, an example of a typical method of preparation of the catalyst comprises the following stages:

(a) synthesis of zeolite MTT with a small crystallites in aqueous solution;

(b) mixing crystalline zeolite MTT with a precursor of the refractory carrier on the basis of inorganic oxide and an aqueous solution to obtain a mixture;

(C) extrusion or molding of the mixture from stage (b) obtaining the extrudate or formed particle;

(d) drying the extrudate or formed particle from step (C);

(e) calcining the dried extrudate or formed particle from step (d);

(f) impregnating the calcined extrudate or formed particle from step (e)at least one metal selected from the group comprising Ca, Cr, Mg, La, Ba, Na, Pr, Sr, K and Nd, with the receipt of the modified metal extrudate or formed particle;

(g) drying the modified metal or molded extrudate particles from step (f);

(h) additional impregnation of the modified meta is scrap extrudate or formed particle from step (g) a metal of group VIII obtaining a catalyst precursor;

(i) drying the catalyst precursor from step (h); and

(j) calcining the dried catalyst precursor from step (i) with getting ready the associated catalyst.

The use of the active material in combination with a synthetic molecular sieve, i.e. United with him, helps to improve the conversion and selectivity of the catalyst in some of the processes of transformation of organic compounds. Examples of active materials are hydrogenated components and metals, added to the impact on the overall activity of the catalyst. In one embodiment of the invention the effect of a catalyst includes acceleration isomerization and reduction kekirawa activity.

In one embodiment of the invention the crystalline molecular sieve of the MTT can be used in close combination with a hydrogenating components for those applications 1 applications where it is desirable gidriruemyi-dehydrogenative action. Typical hydrogenating components may include hydrogen, ammonium, cations of metals such as rare earth metals of group IIA and group VII, and mixtures thereof. Examples hydrogenating component-based metals include tungsten, vanadium, molybdenum, rhenium, Nickel, cobalt, chromium, manganese, platinum, palladium or other noble metals). In one embodiment, the wasp is estline of the invention the metal of group VIII is a noble metal, selected from the group comprising platinum, palladium, rhenium and mixtures thereof. In another embodiment of the invention the metal of group VIII is a noble metal selected from the group comprising platinum, palladium and mixtures thereof. In one embodiment of the invention hydrogenating component-based metal type so that it is approximately 0.3 to approximately 5% of the mass. catalyst calculated on the dry matter.

Metals that are added to influence the overall function of the catalyst (including the acceleration of isomerization and reduction kekirawa activity)include magnesium, lanthanum and other rare earth elements, barium, sodium, praseodymium, strontium, potassium and neodymium. Other metals that can also be used to influence the overall function of the catalyst include zinc, cadmium, titanium, aluminum, tin and iron.

Cation of hydrogen, ammonium, and metal components can be replaced in the molecular sieve. The zeolite may be impregnated with metals or metals can be physically intimately mixed with the molecular sieve using standard methods known in this field. Metals can be occluded in the crystal lattice by introducing desirable metals contained in the form of ions in the reaction mixture from which the zeolite.

In one of the variations is the embodiment of the invention considered zeolite molecular sieve is transformed into its acid form, and then mixed with a precursor of the refractory carrier on the basis of inorganic oxide and an aqueous solution with formation of a mixture. In one embodiment of the invention an aqueous solution is acidic. The aqueous solution acts as peptizyme agent. In one embodiment of the invention the carrier (also known as a matrix or binder) is resistant to the temperatures and other conditions used in the processes of organic transformations. These matrix materials include active and inactive materials and synthetic or natural zeolites as well as inorganic materials such as clays, silica and metal oxides. In one embodiment of the invention the carrier is a natural material. In another embodiment of the invention the carrier is in the form of gelatinous precipitation, sols or gels including mixtures of silica and metal oxides.

In one embodiment of the invention the molecular sieve consists of a porous matrix materials and mixtures of matrix materials such as silicon dioxide, aluminum oxide, titanium dioxide, magnesium oxide, silica-alumina, silica-magnesia, silica-Zirconia, silica-oxide of thorium, silicon dioxide-oxides of beryllium, silicon dioxide-titanium dioxide is, Titania-Zirconia as well as ternary compositions such as silica-alumina-oxide of thorium, silica-alumina-Zirconia, silica-alumina-magnesia and oxide-magnesium oxide-zirconium dioxide. The matrix can be in the form of Kohala. In one embodiment of the invention the matrix materials are aluminum oxide and silicon dioxide.

Inactive materials suitably serve as diluents to control the amount of the conversion in a given process so that products can be obtained economically without the use of other means for regulating the speed of the reaction. Often the materials of the zeolite embedded in the clay of natural origin, such as bentonite and kaolin. These materials, such as clays, oxides, etc., partially act as binders for the catalyst. It is desirable to obtain a catalyst with good crushing strength, because when refining the catalyst is often subjected to harsh conditions of transportation. It contributes to the destruction of the catalyst with the formation of powders that cause problems during processing.

"Modified metal" in this document means that the catalyst on the basis of the molecular sieve contains at least one metal, selected the C group, including Ca, Cr, Mg, La, Na, Pr, Sr, K and Nd; and at least one metal of group VIII. Metals of group VIII are Fe, Co, Ni, Ru, Rh, Pd, Os, Ir and Pt.

In one embodiment of the invention the clay of natural origin combined with synthetic crystalline MTT molecular sieves. Examples of clays of natural origin include the montmorillonite and kaolin family, which families include potentiality and the kaolins commonly known as Dixie, McNamee, Georgia and Florida clays or others in which the main constituent mineral is halloysite, kaolinite, dicit, nacrite or anoxic. Fibrous clays such as thick and attapulgite, can also be used as carriers. These clays can be used in their original state after extraction or can be initially subjected to calcination, acid treatment or chemical modification.

The mixture of molecular sieve and a binder can be prepared in the form of a large number of different physical forms. Generally speaking, the mixture can be in the form of powder, granule, or a molded product, such as extrudate having particle size sufficient to pass through the sieve size 2.5 mesh (Tyler), and stays on the sieve of 48 mesh (Tyler). In cases where the catalyst is molded, for example, by extrusion with an organic binder, the MCA is ü can be extruded before drying or dried or partially dried, and then extruded. Small crystal MTT molecular sieve can also be steamed. Steam treatment helps to stabilize the crystal lattice from exposure to acids. Then the dried extrudate is subjected to heat treatment using the methods of roasting.

In General, it is desirable to minimize the amount of molecular sieve in the final catalyst for economic reasons. Desirable lower levels of molecular sieve in the final catalyst, if achieved good activity and selectivity. In one embodiment of the invention, the content of the molecular sieve has a value of between 5 and 85% of the mass. or in another embodiment, the invention is a value between 5 and 60% of the mass. The content of the molecular sieve varies for different types of molecular sieves.

In one embodiment of the invention, a modified crystalline metal MTT catalyst gives excellent yields and exceptional viscosity index (IV) various kinds of raw materials. The selectivity to by-product is significantly changed compared to catalysts containing a standard MTT zeolite type, for example, the catalyst provides a very low gas formation and education of naphtha. For example, paraffin 500N hydrocracked with the Riez containing 21% of wax, with VI paraffinic feedstock 122, gives a yield of 97% in the pour point of -15°C and VI 120-121. Usually there is a much greater difference from VI paraffinic feedstock to VI deparaffinizing raw materials. For example, when using a catalyst containing a standard MTT zeolite type VI obtained product is approximately 111. Modified metal standard MTT zeolite type network 115 VI. The formation of gas and naphtha is significantly reduced when using crystalline MTT molecular sieve, which is rich in metals. This high output and VI product, very close to VI paraffinic feedstock after dewaxing, was quite unexpected. The yield on the basis of 700°F+ (371,11°C+) deparaffinizing lubricating oil in this case is of such great value as 97%. Moreover, the angle dependence of the VI product temperature fluidity is unusual in that it is not reduced at lower temperature fluidity.

Data have also been obtained for 150N paraffin product of hydrocracking, which similarly indicate improved yield and VI compared with previous catalysts MTT type. And in this case, the observed reduced formation of gas and naphtha. Experienced also MN raw materials and re-watched improved output and VI.

When paraffin cheese is e Fischer-Tropsch were processed using catalyst containing a crystalline molecular sieve of the MTT, rich in metals, obtained 650°F.+ (343°C.+) product was of exceptional value VI 165-170 at temperatures yield between 25 and 30°C. When the product, boiling at 750°F+ (399°C), then split into two fractions, fraction of 750-850°F (399-454°C) had a kinematic viscosity at 100°C 3,8 mm2/C and very high VI 151 at a temperature fluidity -18°C and the fraction of 850°F.+ (454°C.+) had a viscosity of 9.7 mm2/s, temperature fluidity -11°C and 168 VI. Kinematic viscosity was measured according to ASTM D445-06, the pour point was measured according to standard ASTM D5950-02 and VI were measured according to standard ASTM D2270-04.

RAW materials

In one embodiment of the invention used in a method comprising using a catalyst comprising a molecular sieve having a crystalline MTT topology and rich metals, for dewaxing a variety of feedstocks ranging from relatively light distillate fractions such as kerosene and jet fuel to the high-boiling feedstock, such as whole crude oil, recovered oil, the remains of vacuum towers, cycle oils, synthetic oil (e.g., shale oil, tar and oil etc), gas oils, vacuum gas oils, paraffin swelling, waxes, Fischer-Tropsch and intermediate products, crude paraffin, purified AF is La crude paraffin, purified lubricants waxes, n-paraffin waxes, NAO waxes, waxes obtained by chemical processing plants, free from oil waxes, derived from oil, microcrystalline waxes, other heavy oils and mixtures thereof.

In one embodiment, the invention is a raw material hydrocarbon, containing the mass percentage of wax, at least 5%.

The mass percentage of wax in raw materials is measured by heating a sample of the wax up until its temperature is slightly exceed the temperature fluidity, pour 100 grams of sample is heated wax in a calibrated 1-liter beaker and the determination of the mass of the sample heated wax with accuracy to two decimal places; the addition of 400 ml of a mixture of 1:1 toluene:ethyl ketone (MEK) in a glass and dissolution of the sample of wax with gentle stirring to the heated tile to the formation of homogeneous mixture. Cover the beaker with a piece of aluminum foil and put it in the refrigerator set at a temperature fluidity of the raw material. The sample left overnight in a calm state. After cooling in the refrigerator overnight, the mixture is filtered using a filtering device installed in the refrigerator. Use a paper filter from Whatman No. 4 (18.5 cm in diameter) with a Buechner funnel and cover the funnel with a piece of aluminum foil to prevent the collection of ice crystals in the orange. Perform filtering, connecting the funnel with suction pump, high vacuum, pre-moistened filter paper cold MEK, creating a vacuum, quantitatively transferring all the mixture from the beaker into the funnel with a spatula, washing out a glass of cold MEK and filtering the washing liquor. Close the fridge and wait for complete draining of the solvent through the filter, reduce the temperature in the refrigerator to its original temperature. Carefully wash out the wax precipitate on the filter with cold MEK. Allow the precipitate on the filter to dry, disconnect the vacuum and remove the filter funnel out of the fridge. With a spatula transfer the largest possible amount of wax from the filter into the beaker. Removing the last traces of the filtered wax hot toluene and transferred to the washing solution in the beaker. Evaporate the toluene and weigh the wax collected in a measuring Cup. Pour the oily filtrate in a volumetric flask. The solvent is evaporated using a rotary evaporator, weigh the flask plus the remaining oil and determine the weight of oil. The percentage of wax is a lot of wax collected in a measuring Cup, divided by the mass of the sample heated wax, multiplied by 100.

Linear chain n-paraffins either alone or with a slightly branched chain paraffin, soda is containing 16 or more carbon atoms, sometimes herein referred to as waxes. Raw materials will often be a C10+ feedstock generally boiling at temperatures above approximately 350°F (177°C), since lighter oils typically will not contain significant quantities of waxy components. However, the process is particularly suitable for use with recycled raw materials based on paraffin distillates, such as materials based on the average of distillates, including gasoil, kerosene and jet fuel, raw materials for lubricating oils, heating oil and other distillate fraction whose temperature fluidity and viscosity must be maintained within certain limits of the specifications. Raw materials for lubricating oils typically will boil at temperatures above 230°C (450°F), more traditionally at temperatures above 315°C (600°F). Hydrogenated type of recyclable raw materials are a convenient source of raw materials of this type, as well as other fractions of the distillate, as they usually contain significant amounts of waxy n-paraffins. Raw materials of this method will typically be a C10+ feedstock containing paraffins, olefins, naphthenes, aromatics and heterocyclic compounds and with a substantial proportion of heavier n-paraffins and slightly branched paraffins, which define the waxy nature of the feedstock. In the processing of the n-pair the ins and slightly branched paraffins undergo some cracking or hydrocracking to form a liquid material, which contribute to a low viscosity product. The degree of proceeding of cracking, however, is limited, so that the yield of products having a boiling point below the boiling point of the processed raw material is reduced, which ultimately preserves the economic value of raw materials processed.

Typical types of raw materials processed include hydrogenated or hydrocracked gas oils, hydrogenated, the refined lubricating oils, high viscosity cylinder oil, raw materials for lubricating oils, synthetic oils, paraffin swelling, synthetic oils, Fischer-Tropsch, polyolefins with a high pour point, normal alpha olefin waxes, paraffin wax concentrates, refined from oil waxes, microcrystalline waxes and mixtures thereof.

Wax is Fischer-Tropsch process can be obtained by well known methods, such as, for example, commercial suspension technology Fischer-Tropsch SASOL®, a commercial method of synthesis of middle distillate (SMDS) SHELL® or non-commercial progressive gas conversion method (AGC-21) EXXON®. Details of these and other processes are considered, for example, in EP-A-776959, UZ-f-668342, U.S. patent No. 4943672, 5059299, 5733839, and RE39073; and published application U.S. No. 2005/0227866, WO-A-9934917, WO-A-9920720 and WO-A-05107935. The products of the Fischer-Tropsch synthesis generally include hydrocarbons containing from 1 to 100 or even more than 100 carbon atoms and usually include paraffins, olefins and oxygendemand products. the Fischer-Tropsch process is a viable process of formation of clean alternative hydrocarbon products, including waxes, Fischer-Tropsch.

CONDITIONS

The conditions in which the process isomerization dewaxing typically include temperature, which lies in the range of from about 392°F (200°C) to about 820°F. (438°C)and a pressure from about 15 to about 3000 psig (1,055-210 kg/cm2). Typically, the pressure is from about 100 to about 2500 psig (7.03 is-175,78 kg/cm2). Hourly space velocity of the liquid during contacting is generally from about 0.1 to about 20, for example from about 0.1 to about 5. In one embodiment of the invention, the contacting is performed under hydrogen pressure. The ratio of hydrogen to hydrocarbon may be in the range from about 2000 of them (56.6 cubic meters) to about 10000 (283,2 cubic meters) standard cubic feet of H2per barrel of hydrocarbon (159 l), for example from about 2500 (70,8 cubic meters) to about 5000 (141,6 cubic meters) standard cubic feet of H2per barrel of hydrocarbon (159 l).

In one embodiment of the invention the product isomerization dewaxing further treated, nab is emer, Hydrotreating or adsorption treatment. The Hydrotreating is conveniently carried out in the presence of a metallic hydrogenation catalyst, such as platinum on alumina. Hydrotreating can be performed at a temperature of from about 374°F (190°C) to about 644°F (340°C) and a pressure of from about 400 psi (28 kg/cm2) to about 3000 psi (211 kg/cm2). Hydrotreating in this form is a process described, for example, in U.S. patent 3852207, which was put into this document by reference.

EXAMPLES

Another term that can be used to describe crystalline MTT molecular sieve, is rich in metals, "modifier". Synthesis modifier (about x-rays) on the basis of the crystalline molecular sieve is similar to the crystallization of a sample of zeolite with very small crystals. Radiograph expands with decreasing crystallite size. In General, for systems MTT molecular sieves with decreasing relationship SiO2/Al2O3(higher % of the mass. Al in the zeolite), the crystallite size decreases.

Table 2(a) lists the peaks and the relative intensity of the peaks corresponding standard molecular sieve SSZ-32. Table 2(b) lists the peaks and the data on the intensity of the crystalline peaks MTT the Molek is popular sieves before saturation of the metal. Table 2(b) width of the peak, so that the main peaks MTT molecular sieves with small crystallites and standard SSZ-32 easy to compare.

Table 2(a)
The list of peaks of the standard SSZ-32
2 thetaThe grating pitch d,
(Å)
Relative intensity (%) (I/I0)×100
7,911,219
8,210,824
8,910,011
11,47,820
14,76,052
15,95,595
11,45,414
18,24,8812
19,6to 4.5269
20,14,4311
20,94,2570
21,44,159
22,83,90100
23,9to 3.7353
24,03,7058
24,73,6150
25,23,5336
26,03,4342
28,23,1611
29,43,037
31,62,8313

Table 2(b)
Peaks their malconditions the CSOs MTT molecular sieve
2 thetaThe grating pitch d,
(Å)
Relative intensity (%) (I/I0)×100
8,0311,033
8,8310,06
11,307,8320
15,715,643
16,345,423
18,094,907
19,544,5433
19,674,5120
20,814,2731
21,214,1814
22,743,9163
23,913,72100
3,6224
25,093,5534
25,873,4431
26,913,315
28,103,174
29,343.04 from5
31,462,848
31,942,803
34,022,631
35,222,5517
36,292,4716

Figure 11 presents the x-ray data of two types MTT molecular sieves, which are plainly visible to the broader peaks on the x-ray MTT molecular sieves with small crystallites.

EXAMPLE 1. SYNTHESIS of CRYSTALLINE MTT MOLECULAR SIEVE

MTT molecular sieve with small crystallites with what was ndesirable as follows. Used the liner Hastelloy C autoclave with a capacity of 5 gallons (18,95 liters) for mixing reagents and subsequent thermal processing. With a speed of 1500 rpm for ½ hour mixing the following components, as soon as they were entered in the order they are presented: 300 grams of 1-molar solution of hydroxide, N,N'-diisopropylidene mixed with 4500 grams of water. The iodide salt was prepared as in U.S. patent 4483835, example 8, and then was carried out by ion exchange to obtain the hydroxide form using ion-exchange resin BioRad AG1-X8. Added 2400 grams of 1N solution of KOH. Added 1524 grams of Ludox AS-30 (30% of the mass. SiO2). Introduced 1080 grams of colloidal Zola Nalco 15=056 (20% of the mass. SiO2and 4% of the mass. Al2O3). And, lastly, to the mixture was added 181 grams of isobutylamine. The molar concentration of amine Qb exceed the molar concentration of the compound imidazole Qa.

Once the mixing was completed, the lid of the autoclave was closed and the reaction was performed at 170°C for 8-hour period. The system was stirred at 150 Rev/min. the Reaction was interrupted and the product was collected after 106 hours of heating. The precipitate was collected by filtration (which was very slow, indicating small crystals). Then the precipitate was washed several times, and then dried. The dried material was analyzed by the method of x-ray diffraction, and x-rays are shown is table 3. The comparison with the data for the standard SSZ-32, shown in table 2(a), where you can see that the new product of example 1 is similar to that of SSZ-32, but has a diffraction line of x-rays is much wider.

Table 3
The grating spacing d (Å)IntensityRelative intensity (%) (I/I0)×100
8,0011,051526
8,80of 10.05610
11,307,831017
14,506,1112
of 15.755,6335
16,50lower than the 5.3735
18,104,901 712
19,534,5454171
20,054,4286 shoulder10 shoulder
20,774,2774171
21,304,171712
22,713,91558100
23,883,7265798
a 24.573,6233052
25,083,5512543
25,883,4432747
26,883,31759
28,11 3,174610

To find out whether the product is a mixture of small crystals and amorphous material of considerable size, were analyzed by THE method (transmission electron microscopy). The operation of the microscope showed that the product of example 1 were relatively homogeneous crystalline MTT molecular sieve with very little evidence of the presence of amorphous material. The crystallite-characterized by a distribution of small, wide strojcompany components having a diameter in the range of from about 200 to about 400 Å in the longest direction. The ratio of SiO2/Al2O3this product was 29.

EXAMPLE 2

The product of example 1 was progulivali at 1100°F (593,3°C) in air at a heating rate of 1 deg/min (1.8 to F/min), in a stationary mode at 250°F (121, 1million°C) for 3 hours, 1000 F (537,7°C) for 3 hours and then 1100°F (593,3°C) for 3 hours. The calcined material retained its crystallinity by x-ray. The calcined zeolite was subjected to 2 cycles of ion-exchange treatment at 200°F (93,3°C) (using NH4NO3). As described previously in U.S. patent No. 5252527, the material after ion-exchange treatment was re-progulivali, and then measurements of microscopic pores, using the method of the study is also described in 5252527. New product, crystalline MTT molecular sieve, unexpectedly differed from the traditional SSZ-32.

The degree of adsorption of Ar crystalline MTT molecular sieve (Ar adsorption at C relative pressures of 0.001 and 0.1)/(total adsorption of Ar to a relative pressure of 0.1) is greater than 0.5. In one embodiment of the invention, the degree of adsorption of Ar lies in the range from 0.55 to 0.70. Unlike standard SSZ-32, the degree of adsorption of Ar is less than 0.5, typically between 0.35 and 0.45. Small crystal MTT molecular sieve of examples 1 and 2 showed the degree of adsorption of Ar 0,62.

The external specific surface area of the crystallites increased from approximately 50 m2/g (SSZ-32), 150 (small crystal MTT molecular sieve) m2/g, indicating substantial outer surface as a result of the presence of small crystals. At the same time, the volume of micropores for crystalline MTT molecular sieve dropped to approximately a 0.035 CC/g, compared with approximately 0,06 CC/g for standard SSZ-32.

EXAMPLE 3

Crystalline MTT zeolite was mixed with aluminum oxide, extrudible, dried and progulivali. The dried and calcined extrudate was impregnable solution containing platinum and magnesium, and then finally dried and progulivali. The total content of platinum sostav the lo 0,325% of the mass. This modified metal catalyst was then tested on the degree of isomerization of paraffin 500N hydrocracked feedstock, containing 21% of wax, a kinematic viscosity at 100°C 10218 mm2/s, and temperature yield strength +51°C. is Used, the conditions of the isomerization process was LHSV of 1.0 h-1the ratio of gas to oil 4000 SCF/bbl (0,7 CBM/l) and total pressure of 2300 psi (of 161.7 kg/cm2). After isomerization products were subjected to hydrofining over the Hydrotreating catalyst Pt/Pd silicon dioxide aluminum oxide at 450°F (232,2°C). VI paraffin 500N hydrocracked feedstock was 122, and VI deparaffinizing solvent paraffin 500 N geokriminogennoe raw material was 106 when the solvent was deparaffinization at -18°C. the Difference between VI paraffinic feedstock and VI catalytically isomerizing product was only two (122-120)that was exceptional.

Figure 1 and 2 shows the output, and the VI of the product depending on the temperature fluidity, achieved with modified metal catalyst comprising a catalyst based on crystalline MTT zeolite ("modified metal SSZ-32X"). Data at different temperatures yield and the corresponding viscosity indices were obtained by changing the operating temperature of the dewaxing catalyst (for example, more than the low temperature fluidity is achieved when the temperature of the catalyst). The comparison of the results for the other two catalysts, a standard MTT-containing catalyst ("standard SSZ-32") and a modified metal standard MTT-containing catalyst ("modified metal SSZ-32"), tested under the same conditions and on the same raw materials. Isomerization yield of product boiling at 700°F (371,1°C) and above, when using the modified metal catalyst comprising crystalline MTT zeolite catalyst at a temperature fluidity typical of the product in the specified range from -12 to -15°C was unprecedented 96-97%. VI product was approximately 120, which is also excellent, and I believe that this is due to the exclusive access isomerizing wax remaining in the product with a boiling range of base oil. The slope of the dependence of the VI of the product, boiling at 700°F (371,1°C) and higher temperature yield strength was negative, approximately -0,15 so that VI has really increased with the decrease of temperature fluidity. Example 3 shows where two or more isomerized product, boiling at 343°C (650°F) or above, have an appropriate viscosity index 104, 110 or above. Figure 3 and 4 show low outputs C1-C4products ("Blowing") and C5-C250°F(121, 1million°C)products (nafta), achieved with modified metal cat is a lyst including the catalyst based on crystalline MTT zeolite ("modified metal SSZ-32X"), in comparison with the other two catalysts.

EXAMPLE 4

The same modified metal catalyst from example 3 was tested in the isomerization on paraffin 150N hydrocracked feedstock containing 10% wax and having a temperature fluidity of +32°C. the Used conditions of the isomerization process was LHSV of 1.0 h-1the ratio of gas to oil 4000 scout/barrel (0,7 CBM/l) and total pressure of 2300 psi (of 161.7 kg/sq.m). After isomerization products were subjected to hydrofining over the Hydrotreating catalyst Pt/pd silicon dioxide aluminum oxide at 450°F (232,2°C).

Figure 5 and 6 shows the output, and the VI of the product depending on the temperature fluidity achieved when using modified metal catalyst comprising crystalline MTT zeolite catalyst ("modified metal SSZ-32"). The comparison of the results for the other three catalysts: standard MTT-containing catalyst ("standard SSZ32"), modified metal standard MTT-containing catalyst ("modified metal SSZ-32") and standard crystalline MTT zeolite catalyst that has not been modified metal ("crystalline SSZ-32X"). All four produce the RA was tested in the same conditions and using the same 150N raw materials. Isomerization yield of product boiling at 650°F (343°C) and above, when using the modified metal catalyst comprising crystalline MTT zeolite catalyst at a temperature fluidity typical of the product in the specified range from -12 to -15°C ranged from 94 to 95%. VI product amounted to approximately 108. The slope of the dependence of the VI of the product, boiling at 650°F (343°C) and higher temperature yield strength was approximately 0,09, which is considerably less than that obtained with the catalysts of comparison. VI has not decreased much, and decreased temperature fluidity, when using the modified metal catalyst comprising crystalline MTT zeolite catalyst. 7 and 8 show low outputs1-C4products ("Blowing") and C5-C250°F(121, 1million°C)product (nafta)achieved when using modified metal catalyst comprising crystalline zeolite catalyst ("modified metal SSZ-32X"), in comparison with the other two catalysts.

EXAMPLE 5

The same modified metal catalyst from example 3 was also tested in the isomerization process using paraffin medium neutral (220N, MN) raw material containing 12.2% of wax having a kinematic viscosity at 100°C 6,149 mm2/s and so is the temperature value yield +39°C. Used conditions of the isomerization process consisted of 1.6 LHSV h-1the ratio of gas to oil 4000 scout/bbl (0,cubm/l) and total pressure of 2300 psi (of 161.7 kg/m2). After isomerization products were subjected to hydrofining over the Hydrotreating catalyst Pt/Pd silicon dioxide aluminum oxide at 450°F (232,2°C).

Figure 9 and 10 shows the dependence of the yield and VI product temperature yield strength obtained using the modified metal catalyst comprising crystalline MTT zeolite catalyst ("modified metal ("SSZ-32"). The comparison of the results for the other two catalysts: the standard MTT-containing catalyst ("standard SSZ-32") and a modified metal standard MTT-containing catalyst ("modified metal SSZ-32"). All three catalysts were tested in the same conditions and using the same 220N raw materials. Isomerization yield of product boiling at 650°F (343°C) and above, when using the modified metal catalyst comprising crystalline MTT zeolite catalyst at a temperature fluidity typical product given interval of -15°C was approximately 92%. VI product was 105. The slope of the dependence of the VI of the product, boiling at 650°F (343°C) and higher temperature yield strength in the range of those which of erator yield from -12°C to -22°C was almost equal to zero, which again was significantly lower than those obtained with catalysts of comparison. VI is not reduced at lower temperature yield strength in the case of the modified metal catalyst comprising crystalline MTT zeolite catalyst.

EXAMPLE 6

The same modified metal catalyst from example 3 was tested in the isomerization process on gidrirovaniem paraffin raw Fischer-Tropsch containing more than 90% of the wax, manufactured by suspension technology Fischer-Tropsch SASOL®. Used conditions of the isomerization process included a LHSV of 1.0 h-1the ratio of gas to oil 5000 scout/barrel (0,88 CBM/l) and total pressure 300 psi (21 kg/cm2). After isomerization products were subjected to hydrofining over the Hydrotreating catalyst Pt/Pd silicon dioxide aluminum oxide at 450°F (232,2°C). The products obtained, boiling at 650°F (343°C) and above, had a VI from 165 to 170 at the temperature fluidity between -25 and -30°C. the Yield of products boiling at 650°F (343°C) and above was higher than 65% of the mass. when the temperature fluidity 20°C. the Products boiling at 650°F (343°C) and above, were further separated by vacuum distillation into two fractions, one boiling between 750 and 850°F (399 451°C), and another, boiling at 850°F (451°C) and above. More boiling fraction had a kinematic viscosity at 100°C 3,8 mm2/s, VI 151 and temperature fluidity -18°C. More in cookipedia fraction had a kinematic viscosity at 100°C 9.7 mm 2/s, VI 168 and temperature fluidity -11°C. Comparative experience with the use of the modified metal standard MTT-containing catalyst under the same process conditions and on the same raw materials gave lower yields, but the slightly higher value of VI. It is interesting to note that even if VI were slightly lower when using modified metal crystalline MTT zeolite catalyst, the slope of the dependence of the VI of the product, boiling at 650°F (343°C) and higher temperature yield strength at the temperature fluidity from -20°C to -50°C was significantly less than, less than 0,56 than the slope obtained with the catalyst of comparison, more 0,72.

1. A method of obtaining a base oil, comprising contacting the C10+hydrocarbons with a catalyst and hydrogen at isomerization conditions to obtain base oils, where the catalyst includes a molecular sieve having the topology structure of the MTT and the diameter of the crystallites from 200 to 400 Å in the longest direction, at least one metal selected from the group consisting of Ca, Cr, Mg, La, Na, Pr, Sr, K and Nd, and at least one metal of group VIII.

2. The method according to claim 1, where the stage contacting is carried out at a temperature 200-427°C (392-800°F) and pressures from 103,4 kPa (15 psi) to 20,685 kPa (3000 psi), and hourly volumetric velocity of the fluid from 0.1 to 20.

3. The method according to claim 1, the de C 10+hydrocarbon feedstock is a heavy neutral raw materials.

4. The method according to claim 3, where the base oil is a base oil, group III.

5. The method according to claim 3, where the base oil is 97% at a temperature fluidity -15°C.

6. The method according to claim 1, where C10+hydrocarbon is the average neutral raw materials.

7. The method according to claim 6, where the base oil is a base oil group II.

8. The method according to claim 6, where the base oil is 92% at a temperature fluidity -15°C.

9. The method according to claim 1, where C10+hydrocarbon feedstock is a light neutral raw materials.

10. The method according to claim 6, where the base oil is 94% at a temperature fluidity -15°C.

11. The method of dewaxing a hydrocarbon feedstock with getting isomerizing product, the raw material contains a linear chain and slightly branched paraffins containing 10 or more carbon atoms, including the implementation of contact of the feedstock in the isomerization conditions in the presence of hydrogen with a catalyst comprising a molecular sieve having the topology structure of the MTT and the diameter of the crystallites of approximately 200 to approximately 400 Å in the longest direction, the catalyst contains at least one metal selected from the group comprising Ca, Cr, Mg, La, Na, Pr, Sr, K and Nd, and at least one metal of group VIII.

12. The method according to claim 11, where MTT molecular the second sieve selected from the group comprising SSZ-32, ZSM-23, EU-13, ISI-4, KZ-1.

13. The method according to claim 11, where the specified raw materials selected from the group comprising hydrogenated or hydrocracked gas oils, hydrogenated, the refined lubricating oils, light products, raw materials for lubricating oils, synthetic oils, paraffin swelling, synthetic oils, Fischer-Tropsch, polyolefins with high temperature yield strength, normal alpha olefin waxes, paraffin wax concentrates, refined from oil waxes, microcrystalline waxes and mixtures thereof.

14. The method according to claim 11, where the metals of group VIII selected from the group comprising platinum and palladium and mixtures thereof.

15. The method according to claim 11, where the specified contact is carried out at a temperature 232-427°C (450-800°F) and pressures from about 103,4 kPa (15 psi) to about 20,685 kPa (3000 psi).

16. The method according to clause 15, where the specified pressure is in the range from approximately 689,5 kPa (100 psi) to approximately 172 37 Daphne-Athens kPa (2500 psi).

17. The method according to clause 15, where hourly space velocity of the liquid at the time of contact is from about 0.1 to about 20.

18. The method according to 17, where hourly space velocity of the liquid is from 0.5 to about 5.

19. The method according to claim 11, where hydrocarbons hydronaut before isomerization at a temperature of from 163 to 427°C (325-800°F).

20. The method according to claim 11, further include the second stage Hydrotreating followed by isomerization.

21. The method according to claim 20, where the Hydrotreating is carried out at a temperature of from about 163 to about 310°C (325 to about 590°F) and pressures of about 2068 kPa (300 psi) to approximately 20685 kPa (3000 psi).

22. The method according to claim 11, further comprising Hydrotreating isomerizing product.

23. Method of dewaxing, including isomerization the dewaxing of hydrocarbons containing at least 5 wt.% wax, over the catalyst, where the catalyst includes a molecular sieve having the topology structure of the MTT and the diameter of the crystallites from 200 to 400 Å in the longest direction, at least one metal selected from the group comprising Ca, Cr, Mg, La, Na, Pr, Sr, K and Nd, and at least one metal of group VIII, obtaining two or more isomerized product, boiling at 343°C (650°F) or above, each isomerized product has
a) the temperature fluidity between 0 and -30°C and
b) corresponding to the viscosity index of 95 or higher
where a straight line, built to the temperature dependence of yield strength on the x-axis and viscosity indices on the y-axis gives the slope for y is zero or less.

24. Method of dewaxing according to item 23, where the hydrocarbon feedstock is at least 10 wt.% the wax.

25. Method of dewaxing according to item 23, where the hydrocarbon feedstock has a kinematic viscosity at 100°C 2.5 mm2 /s or more.

26. Method of dewaxing according to item 23, where two or more isomerized product, boiling at 343°C (650°F) or above, have an appropriate viscosity index 104 or higher.

27. Method of dewaxing according to item 23, where the output of the two or more isomerized product, boiling at 343°C (650°F) or above 90 wt.% or more per raw.

28. Method of dewaxing according to item 23, where the output is 94 wt.% or more.

29. Method of dewaxing according to item 23, where the slope of a line is less than -0,05.

30. Method of dewaxing, including isomerization the dewaxing of hydrocarbons containing at least 5 wt.% wax, over the catalyst, where the catalyst includes a molecular sieve having the topology structure of the MTT and the diameter of the crystallites from 200 to 400 Å in the longest direction, at least one metal selected from the group comprising Ca, Cr, Mg, La, Na, Pr, Sr, K and Nd, and at least one metal of group VIII, obtaining two or more isomerized product, boiling at 343°C (650°F) or above, each isomerized product has
a) the temperature fluidity between 0 and -30°C and
b) corresponding to the viscosity index of 95 or higher
where a straight line, based on the temperature dependence of yield strength on the x-axis and viscosity indices on the y-axis gives the slope for y is zero or less and where the output of the TLD is or more isomerized products boiling at 343°C (650°F) or above 90 wt.% or above in the calculation of raw materials.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing base oil, involving: providing a first catalyst containing at least one group VIII metal deposited on a M41S catalyst support, such as MCM-41, and having density of 600 kg/m3 or less; providing a second catalyst containing at least one group VIII metal, having dewaxing efficiency which is sufficient to facilitate treatment of a stream of light neutral (150 N) hydrocarbons from a medium-pressure hydrocracking apparatus, having kinematic viscosity at 100°C of less than 5 and end boiling point lower than 550°C, at 320°C and liquid hourly space velocity (LHSV) of 1 h-1, to obtain base oil having chilling temperature lower than 15°C; bringing the material into contact with the first catalyst at adequate conditions for treating the material, wherein said adequate conditions are adequate for one of the processes selected from hydrotreatment, hydrofining or hydrogenation of aromatic compounds, and bringing the treated material into contact with the second catalyst at conditions adequate for dewaxing the treated material. The invention also relates to another method of producing base oil.

EFFECT: enabling flexible treatment of material with different paraffinicity.

13 cl, 12 dwg, 3 tbl, 19 ex

FIELD: gas and oil production.

SUBSTANCE: invention refers to procedure for oil de-waxing with liquefied propane-butane gas. The procedure consists in addition of depressor additive Flexoil at amount of 0.050-0.1% wt to mixture of oil-liquefied gas. Also, paraffin is separated with filtration.

EFFECT: increased amount of paraffin removed from oil.

2 cl, 12 ex, 1 tbl

FIELD: chemistry.

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17 cl, 1 tbl

FIELD: oil and gas production.

SUBSTANCE: invention relates to petrochemistry field. Invention relates to dewaxing method of fractions of highly paraffinic crude at presence of catalyst, in the capacity of catalyst there are used potassium persulfate (K2S2O8) or acetous manganese (Mn(CH3COO)2), process is implemented during blending at temperature 240-280°C during 12-17 hours with following double-stage fractions distillation, fractions, steamed away up to 450°C with receiving of dewaxing residue.

EFFECT: invention provides dewaxing implementation of hard oil fractions.

7 ex, 1 tbl

The invention relates to equipment for carrying out processes of purification of oil from wax, and in particular to equipment for carrying out processes of extraction of liquid n-paraffin from crude oil by adsorption

FIELD: chemistry.

SUBSTANCE: described is a catalyst which contains at least one IZM-2 zeolite, at least one matrix and at least one metal selected from group VIII, VIB and VIIB metals, wherein said zeolite demonstrates an X-ray diffraction pattern which includes at least bands indicated in the table below:

where FF = very strong; F = strong; m = average; mf = moderately weak; f = weak; ff = very weak, and having a chemical composition expressed on an anhydrous base, in terms of oxide moles, having the following general formula: XO2:aY2O3:bM2/nO, wherein X denotes at least one tetravalent element, Y denotes at least one trivalent element and M denotes at least one alkali and/or alkali-earth metal with valence n, a and b denote the number of moles of Y2O3 and M2/nO, respectively, a assumes a value from 0.001 to 0.5 and b assumes a value from 0 to 1. Also disclosed is use of the catalyst in isomerisation, transalkylation, hydroisomerisation of paraffins, conversion of an aliphatic compound with one alcohol functional group.

EFFECT: obtaining a catalyst with catalytic properties in conversion processes.

17 cl, 5 tbl, 11 ex

FIELD: chemistry.

SUBSTANCE: invention relates to hydrofining catalysts. Described is a bead catalyst for hydrofining oil fractions, which consists of an aluminium oxide support, active components - molybdenum, nickel or cobalt compounds in form of oxides and/or sulphides and, optionally, additional zeolite Y in hydrogen form, which is in form of spherical or elliptical granules, characterised by that the catalyst granules have packed density of 0.4-0.5 g/ml and pore volume of not less than 1.2 ml/g. Described is a method of preparing said catalyst, involving peptisation of the starting powder - an aluminium oxide source with aqueous solution of an organic acid to obtain a pseudo-sol, moulding the obtained pseudo-sol in ammonia solution, drying and calcination of the support with subsequent embedding of active components therein, with optional embedding of zeolite Y in hydrogen form, drying and calcination of the catalyst in an air current, wherein the starting powder - aluminium oxide source used is weakly crystalline pseudo-boehmite; peptisation thereof is carried out using aqueous solution of an organic acid with concentration of 1-15 wt % and granulation (moulding) is carried out by drip moulding with the solid to liquid ratio in the pseudo-sol of not less than 1:2 and pH of the ammonia solution of not less than 11.0.

EFFECT: high activity, selectivity and stability of the catalyst.

3 cl, 1 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to a hydroisomerisation catalyst, a method of producing said catalyst, a method for dewaxing hydrocarbon oil and a method of producing lubricant base oil. Described is a hydroisomerisation catalyst, obtained by calcining a catalyst composition containing an ion-exchanged molecular sieve or a calcined product thereof, wherein the ion-exchanged molecular sieve is obtained by ion-exchanging a molecular sieve in a solution which contains cationic groups, the molecular sieve includes nanocrystals having a pore structure of decahedral rings or octahedral rings and having a ratio of the pore volume to the external surface area ([pore volume]/[external surface area]) from 2.0×10-4 ml/m2 to 8.0×10-4 ml/m2, and contains an organic matrix and at least one metal selected from a group consisting of metals of Groups 8 to 10 of the Periodic Table of the elements, molybdenum and tungsten, deposited on the ion-exchanged molecular sieve or the calcined product thereof. Described is a method of producing the catalyst, involving a step (a) of hydrothermally synthesising a molecular sieve comprising nanocrystals having characteristics given above and an organic matrix; a step (b) of ion-exchanging the molecular sieve comprising an organic matrix in a solution containing a cationic groups to obtain an ion-exchanged molecular sieve; a step (c) of making the ion-exchanged molecular sieve or a calcined product thereof, carrying at least one metal selected from a group consisting of metals of Groups 8 to 10 of the Periodic Table of the elements, molybdenum and tungsten to obtain a catalyst composition; and a step (d) of calcining the catalyst composition. Described is a method of dewaxing hydrocarbon oil, involving bringing the hydrocarbon oil containing normal paraffins having 10 or more carbon atoms into contact with catalyst described above in the presence of hydrogen to convert a part of or all of the normal paraffins into isoparaffins. Described is a method of producing lubricant base oil in conditions for conversion of normal paraffins of substantially 100 wt %, the conversion being defined by the formula (1): conversion of normal paraffins (%)=[1-(total wt % of normal paraffins having Cn or more carbon atoms contained in mineral oil after contact)/(total wt % of normal paraffins having Cn or more carbon atoms contained in mineral oil before contact)]×100, where Cn denotes the minimum number of carbon atoms in normal paraffins having 10 or more carbon atoms contained in mineral oil before contact.

EFFECT: obtaining a catalyst with high isomerisation selectivity, stable and high output of hydrocarbon oils, suitable for lubricant base oils.

14 cl, 1 tbl, 8 ex, 2 dwg

FIELD: process engineering.

SUBSTANCE: this invention relates to reductive isomerisation catalyst, dewaxing of mineral oil, method of producing base oil and lubrication base oil. Invention covers reductive isomerisation catalyst. Reductive isomerisation comprises molecular sieve treated by ionic exchange or its calcinated material produced by ionic exchange of molecular sieve containing cationic fragments and using water as the primary solvent, and at least one metal selected from the group consisting of metals belonging to group VIII-X of periodic system, molybdenum and tungsten applied onto molecular sieve treated by ionic exchange, or onto its calcinated material. Dewaxing comprises converting portion of or all normal paraffins into isoparaffins whereat mineral oil containing normal paraffins is brought in contact with abode described reductive isomerisation catalyst in the presence of hydrogen. Invention covers also method of producing lubricant base oil and/or fuel base oil implemented by bringing base oil containing normal paraffins in contact isomerisation catalyst in the presence of hydrogen. Invention covers also method of producing lubricant base oil containing normal paraffins, including 10 or more carbon atoms by bringing it in contact with above describe reductive isomerisation catalyst in the presence of hydrogen in conversion of normal paraffins making in fact 100%.

EFFECT: catalyst with high isomerisation activity and sufficiently low cracking activity at high yield.

22 cl, 8 tbl, 4 ex, 11 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to hydrotreatment processes. Described is a method of removing paraffin from hydrocarbon material, involving reacting the material with a mixture of ZSM-48 catalysts under catalytic paraffin removal conditions for producing material from which paraffin has been removed, where the mixture of ZSM catalysts contains: a) first type ZSM-48 crystals, having molar ratio of silicon dioxide to aluminium oxide equal to 70-110 and containing inoculating crystals different from ZSM-48, and b) second type ZSM-48 crystals which differ from first type ZSM-48 crystals on one or more properties selected from presence of inoculating crystals different from ZSM-48, crystal morphology, higher kenyaite percentage and higher molar ratio of SiO2 to Al2O3.

EFFECT: high efficiency of removing paraffin from hydrocarbon material owing to use of a a highly active catalyst.

16 cl, 1 tbl, 6 dwg, 15 ex

FIELD: chemistry.

SUBSTANCE: invention relates to high activity ZSM-48. Described is a catalyst composition for removing paraffin from hydrocarbon material which contains ZSM-48 crystals, having molar ratio of silicon dioxide to aluminium oxide equal to or less than 110, which does not contain inoculating crystals different from ZSM-48 and does not contain ZSM-50 crystals.The invention also describes a method of producing ZSM-48 crystals contained in the composition described above, involving: preparation of an aqueous mixture of silicon dioxide or silicate, aluminium oxide or aluminic acid, hexamethonium salts and an alkaline base, where the mixture has the following molar ratios: silicon dioxide: aluminium oxide 70-110, base: silicon dioxide 0.1-0.3 and hexamethonium salt: silicon dioxide 0.01-0.05, and heating the mixture while stirring for a period of time and temperature sufficient for formation of crystals. The invention also describes a method of removing paraffin from hydrocarbon material in the presence of the catalyst composition described above.

EFFECT: obtained ZSM-48 crystals and a composition based on said crystals exhibit high activity during removal of paraffin from hydrocarbon material.

29 cl, 1 tbl, 6 dwg, 15 ex

FIELD: chemistry.

SUBSTANCE: invention refers to noble-metal catalyst, to method for making and application thereof. There is disclosed method for making noble-metal catalyst for hydrocarbon conversion, involving the stages as follows: a) preparation of the carrier containing zeolite, chosen from zeolites with medium and large pores and acid sites, at temperature within 423 to 1173 K and optional carrier modification; b) deposition of noble metal chosen from platinum, palladium, ruthenium, rhodium, iridium and their mixtures and combinations, by gas-phase deposition including evaporation of noble metal precursor chosen from β-diketonates and metallocenes, and interaction with the carrier, and c) heat treatment in oxidising or reducing environments. There is disclosed application of noble-metal catalyst produced by the method described above, in ring opening, isomerisation, alkylation, hydrocarbon reforming, dry reforming, hydrogenation and dehydrogenation, and preferentially, in ring opening of naphthenic molecules. Additionally, there is disclosed method for making medium diesel fuel distillate by introducing raw medium distillate into the reactor wherein it reacts at temperature 283-673 K and under pressure 10-200 bar with hydrogen with added noble-metal catalyst produced as described above until ring opening of naphthenes with two or more rings completed to produce isoparaffins, n-paraffins and mononaphthenes within medium distillate.

EFFECT: production of catalyst with improved selectivity for hydrocarbon conversion.

16 cl, 5 tbl, 20 ex

FIELD: chemistry.

SUBSTANCE: said invention relates to method for improvement of loss of mobility temperature of hydrocarbon material obtained by Fischer-Tropsch synthesis, in particular to satisfactory-yield conversion of material with high temperature of mobility loss, at least one fraction of which has low mobility loss temperature and high viscosity index for base oil. Method implies utilisation of dewaxing catalyst, which contains at least one zeolite (molecular sieve) chosen from a group of TON type zeolites (Theta-1, ZSM-22, ISI-1, NU-10 and KZ-2), and at least one ZBM-30 zeolite, at least one inorganic porous matrix, at least one hydrogenating/dehydrogenating element, preferentially from group VIB and group VIII of periodic table.

EFFECT: improved loss of mobility temperature for hydrocarbon material obtained by Fischer-Tropsch synthesis.

14 cl, 7 ex, 1 dwg

FIELD: physics.

SUBSTANCE: dewaxing procedure of raw material produced by Fischer-Tropsch method implies that processed raw materials contact with catalyst containing at least one zeolite ZBM-30, synthesised with triethylene tetramine, at least one hydrogenating- dehydrogenating element preferably selected from elements of group VIB and group VIII of periodic table, and at least one inorganic porous matrix.

EFFECT: good recovery of raw material, raised pour point.

13 cl, 5 ex, 1 dwg

FIELD: petroleum chemistry.

SUBSTANCE: invention relates to microcrystalline paraffin obtained by catalytic hydroisomerization at temperature more than 200°C from FT paraffin having from 20 to 105 carbon atoms. Microcrystalline paraffin is non-liquid at 25°C, but at least pasty with needle penetration less than 100x10-1, measured according to DIN 51579. Disclosed is method for production of microcrystalline paraffin.

EFFECT: microcrystalline paraffin free from naphthenes and aromatics.

17 cl, 1 dwg, 1 tbl, 3 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing a fraction of polymethyl-substituted C18-C36 alkanes of formula: , where n=4-10 by reacting molten atactic polypropylene with atmospheric oxygen at 150-250°C for 1-6 hours with air flow rate of 0.6-1.9 l/min∙kg using secondary low-molecular oxidation products as raw material. The method is characterised by that first, low-molecular products are fractionated collection of the basic fraction at 200-310°C followed by catalytic hydrofining from impurities of alkenes in gas phase or oxidation of alkenes at 100°C with aqueous solution of KMnO4 with weight ratio of the fraction to KMnO4 of 2.5-3.0:1.0, followed by freezing the organic layer at minus 20°C and separating the crystalline water-containing precipitate. The invention also relates to use of said fraction as a chemical marker for hydrocarbon fuels.

EFFECT: disclosed marker has a low cost and high concealment.

2 cl, 5 ex, 1 tbl, 4 dwg

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of separating at least one straight C4-C20 hydrocarbon from a fluid mixture containing said straight hydrocarbon and at least one branched isomer thereof. The method involves a step of bringing the fluid mixture into contact with an adsorbent which contains a porous organometallic skeletal material containing at least one at least bidentate organic compound, having a coordination bond with at least one metal ion for adsorption of the straight hydrocarbon, where the at least one at least bidentate organic compound is a monocyclic, bicyclic or polycyclic ring system and is unsubstituted or has one or more substitutes, independently selected from a group consisting of a halogen atom, C1-6-alkyl, phenyl, NH2, NH(C1-6-alkyl), N(C1-6-alkyl)2, OH, O-phenyl and OC1-6-alkyl, where the substitutes C1-6-alkyl and phenyl are unsubstituted or have one or more substitutes, independently selected from a group consisting of a halogen atom, NH2, NH(C1-6-alkyl), N(C1-6-alkyl)2, OH, O-phenyl and OC1-6-alkyl, wherein the ring system of the at least one at least bidentate organic compound is a substituted imidazole, and where said at least one metal ion is an ion of a metal selected from a group consisting of Zn, Cu, Co, Ni, Fe and Mn. The invention also relates to use of said porous organometallic skeletal material in the method of separating straight hydrocarbons from branched isomers thereof.

EFFECT: present invention provides an alternative, easily to make absorbent.

9 cl, 4 ex, 3 dwg

FIELD: explosives.

SUBSTANCE: invention relates to the method for selective production of hydrocarbons suitable for use as diesel fuel, consisting in decarbonylation / decarboxylation of a mixture of carbonic acids C8-C24 (saturated and non-saturated) in a dissolvent in hydrogen atmosphere in presence of a heterogeneous catalyst representing palladium on aluminium oxide at the temperature of 200-400°C and pressure of 0.1-5 MPa. The method is characterised by the fact that a granulated catalyst is used, in which palladium is distributed in the surface layer of the carried with penetration depth of 0.1-0.6 mm and palladium content in the catalyst making 0.25-5 wt %.

EFFECT: invention provides an efficient industrial method for selective production of hydrocarbons from renewable sources using highly efficient catalysts of fatty acids deoxygenation to saturated hydrocarbons suitable for use as components of diesel fuel.

2 cl, 8 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing saturated hydrocarbons - diesel components and fatty acid esters by reacting triglycerides of fatty acids with hydrogen using a copper-containing catalyst. The catalyst is part of a permeable composite material which contains, besides a catalytically active copper compound, copper metal as a reinforcing and heat-conducting component.

EFFECT: use of the present method enables to achieve high degree of conversion of triglyceride of stearic acid to form a mixture of saturated hydrocarbons with boiling point in the range of 200-350°C and fatty acid esters with low content of undesirable substances in the products.

8 cl, 8 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to an oil medium which is suitable for producing dimethyl ether and/or methanol which is used in a synthesis reaction with a suspended layer as a medium which contains a basic component in form of a branched saturated aliphatic hydrocarbon containing 16-50 carbon atoms, 1-7 tertiary carbon atoms, 0 quaternary carbon atoms and 1-16 carbon atoms in branched chains bonded with tertiary carbon atoms; wherein at least one tertiary carbon atom is bonded with hydrocarbon chains with length of 4 or more carbon atoms, lying in three directions. The invention also relates to a method of producing dimethyl ether and a mixture of dimethyl ether and methanol using said oil medium.

EFFECT: use of the present oil medium ensures high efficiency of synthesis.

9 cl, 4 ex, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: at the first step, raw material containing at least one fatty acid, having 8-26 carbon atoms, is esterified with at least one fatty alcohol having 8-26 carbon atoms to obtain esters, at the second step, the obtained esters are hydrogenated to fatty alcohols, at the third step, the obtained fatty alcohols are dehydrogenated to alpha-olefins, at the fourth step, the alpha-olefins are oligomerised to oligomers which are then hydrogenated at the fifth step. The invention also relates to polyolefin base oil or a base oil component obtained using the described method.

EFFECT: invention enables to obtain branched saturated hydrocarbons from renewable sources.

15 cl, 5 tbl, 4 ex, 1 dwg

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