RU2425093C2 - Paraffin hydrocracking method and method for obtaining material of fuel base - Google Patents

Abstract

FIELD: oil and gas industry.

SUBSTANCE: invention refers to paraffin hydrocracking method which consists in passage of olefin-containing paraffin obtained by Fischer-Tropsch synthesis, in presence of hydrogen and in the specified sequence through the first layer of catalyst, which contains catalyst which is considerably devoid of acid functionality, which includes carrier and metal of group VIII, which is applied to the above carrier, and applied amount of this metal is equal to 0.005-0.010 wt %, relative to the above carrier, and the second layer of catalyst, which contains catalyst having activity to hydrocracking and including metal of group VIII, which is applied to the carrier containing solid acid. Invention also refers to the method for obtaining fuel base component.

EFFECT: possibility of maintaining high selectivity of middle distillate and obtaining middle distillate at sufficient output.

4 cl, 3 ex, 1 tbl, 2 dwg

Description

Technical field

The present invention relates to a method for hydrocracking paraffin and to a method for producing fuel base components.

State of the art

Based on the idea of reducing the environmental burden, in recent years there has been a need for environmentally friendly clean fuels, which have a low sulfur content and low aromatic hydrocarbon content. In addition, the regulation of sulfur content in liquid fuels, such as gasoline or diesel fuel, has recently become more relevant; for example, the normative value for sulfur in diesel fuel fell from 500 ppm (ppm) to 50 ppm. Researches, therefore, are directed in the oil sector to Fischer-Tropsch synthesis (hereinafter referred to as “FT synthesis”) as a method for obtaining clean fuel. The raw materials in the Fischer-Tropsch synthesis are hydrogen obtained by gasification of bitumen or coal or reforming of natural gas, and carbon monoxide. Expectations from FT synthesis are very high since it can produce paraffin-rich basic components of liquid fuels that do not contain sulfur. Since paraffin can also be obtained by FT synthesis, this paraffin (in some cases referred to below as “FT paraffin”) can be hydrocracked and this hydrocracked product can also be used as a base component for clean fuels.

When the fuel base component is obtained by hydrocracking paraffin, it is present in the middle distillate of the hydrocracking product, which is the component used as the fuel base component; and, as a result, the yield of this middle distillate is crucial in improving the economic performance of the fuel production process. Hydrocracking methods are therefore introduced to improve the selectivity of the middle distillate during a paraffin hydrocracking process, in which, for example, paraffin is contacted, in the presence of hydrogen, with a catalyst containing crystalline aluminosilicate and a Group VIb metal of the periodic table and / or Group VIII metal (referring, for example, to Patent Links 1-3).

Patent reference 1 WO 2004/028688.

Patent Reference 1. Publication of Japanese Unexamined Patent Application No. 2004-255241.

Patent Document 3. Publication of Japanese Unexamined Patent Application No. 2004-255242.

Disclosure of invention

Problems to be Solved by the Present Invention

However, there is a tendency for the olefin content in FT paraffins to be influenced by differences in the type of catalyst used for the synthesis and the reaction conditions during the synthesis. FT paraffin described above is used as a raw material for clean fuels; however, when during their research the present inventors tried to hydrocrack FT paraffin containing a large amount of olefins, it was found that maintaining high selectivity of the middle distillate was extremely difficult, even using the technology described in Patent Links 1-3, and that as a result the yield of this middle distillate ended in a decrease. Therefore, a technology is required that can appropriately maintain the selectivity of the middle distillate during hydrocracking, even when olefins are present in paraffin, but at present the situation is such that effective methods that can realize this have not yet been developed.

The present invention was carried out on the basis of the circumstances described above, and took as a goal the introduction of a method for hydrocracking paraffin, which is able to maintain the selectivity of the middle distillate at high levels during hydrocracking of an olefin-containing paraffin. An additional objective of the present invention is the introduction of a method for the production of fuel base components that uses this hydrocracking method.

Problem Solving Tools

As a result of studies aimed at solving the problem indicated above, the authors found that the content of middle distillate (fraction with a boiling point of 145 to 360 ° C) in the cracking product can be maintained at a high level by bringing the olefin-containing paraffin into contact with a special catalyst before contacting with a catalyst that has hydrocracking activity, and that as a result, the fraction (middle distillate) that is applicable as a fuel base component can be obtained in good yield m. The present invention has been achieved based on these findings.

In other words, the paraffin hydrocracking method of the present invention is characterized by passing an olefin-containing paraffin in the presence of hydrogen and in a predetermined sequence through a first catalyst bed that contains a catalyst substantially lacking acid functionality and a second catalyst bed that contains a catalyst having hydrocracking activity.

For the purposes of the present invention, “a catalyst substantially lacking acid functionality” means that the catalyst is acidic or, in the case of a catalyst that exhibits acidity, means that the acid located therein does not participate in paraffin isomerization and cracking or does not participate in the polymerization of olefins.

By passing the olefin-containing paraffin through the catalyst beds described above, the hydrocracking process of the present invention can maintain the output of the middle distillate at high levels during the hydrocracking of paraffin and can guarantee the corresponding yields of a component useful as a fuel base component which is obtained from paraffin.

The reason why the present invention achieves the effects described above is not well understood, but the inventors put forward the following hypotheses. First, the root cause of the increased selectivity of the middle distillate is thought to be determined by the increase in the reaction temperature in the catalyst bed caused by the exothermic reaction when the olefins come in contact with a catalyst that has hydrocracking activity. In contrast, the method for hydrocracking the paraffin of the present invention by contacting an olefin with a catalyst bed that contains a catalyst lacking acid functionality is intended to effectively suppress the exothermic reaction in the hydrocracking active catalyst and therefore is capable of appropriately maintaining the selectivity of the middle distillate of the hydrocracking catalyst.

The catalyst contained in the first catalyst layer in the paraffin hydrocracking method of the present invention is preferably a catalyst comprising a support and a Group VIII metal supported on this support, and the amount of supported metal is 0.005-0.010% by weight. in relation to the carrier.

This carrier preferably contains at least one oxide selected from the group consisting of silica, alumina, zirconia.

Paraffin in the paraffin hydrocracking process of the present invention is preferably obtained by Fischer-Tropsch synthesis.

The catalyst contained in the second catalyst bed in the paraffin hydrocracking method of the present invention preferably contains ultra-stable Y-type zeolite.

The present invention also provides a method for producing a fuel base component, characterized by fractional distillation of a hydrocracking product obtained by the paraffin hydrocracking method according to the present invention, as described above, to obtain a fuel base component. This method of producing a fuel base component can produce a fuel base component from an olefin-containing paraffin in an economically advantageous manner.

Effect of the invention

The present invention provides a method for the paraffin hydrocracking, which allows maintaining the selectivity of the middle distillate at high levels during the hydrocracking of an olefin-containing paraffin. The present invention also provides a method for producing fuel base components that uses this hydrocracking method.

Brief Description of the Drawings

Figure 1 is a flow chart that shows one example of a device for the production of liquid petroleum products (fuel base component), which implements the method of the present invention, paraffin hydrocracking.

Figure 2 is a flow chart that shows another example of a device for the production of liquid petroleum products (fuel base component), which implements the method of the present invention, paraffin hydrocracking.

Position Explanations

10, 30, 40: reaction column, 12: first catalyst layer, 14: second catalyst layer, 16: catalyst layer (first catalyst layer), 18: catalyst layer (second catalyst layer), 20: distillation column, 100, 110: device for the production of liquid petroleum products.

The best options for carrying out the invention

Preferred embodiments of the present invention are hereinafter described in detail with reference to the drawings appended here. In the description of the drawings, the same reference signs are assigned to the same or equivalent elements and duplicate descriptions are not given.

The flow chart in Figure 1 shows one example of a liquid petroleum product (fuel base component) manufacturing apparatus that implements the paraffin hydrocracking method of the present invention. The liquid petroleum product manufacturing device 100 shown in Figure 1 is a device that produces an olefin-containing paraffin liquid petroleum product that contains a component used as a fuel base component.

The liquid petroleum product production device 100 shown in Figure 1 is provided with a reaction column 10 that hydrocracks the olefin-containing paraffin and a distillation column 20 for fractionally distilling the desired fractions of the hydrocracking product that passes through the reaction column 10. The feed line L1 is connected to the reaction column 10 to supply paraffin to the reaction column 10, and line L2 is connected to this line L1 to introduce hydrogen there. Paraffin and hydrogen pass through these lines and are fed to the reaction column 10. The lower part of the reaction column 10 is connected to the distillation column 20 by the transport line L3, and the paraffin that has passed through the reaction column 10 (hydrocracking product) is transported through this line L3 to the distillation column 20 .

In this embodiment, the reaction column 10 sequentially from the top of the column includes a first catalyst bed 12 that contains a catalyst substantially lacking acid functionality and a second catalyst bed 14 that contains a catalyst having hydrocracking activity. The paraffin hydrocracking process of the present invention is carried out in this reaction column 10.

The olefin-containing paraffin fed to the reaction column 10 may be paraffin, which preferably contains 10% of the mass. olefins, more preferably at least 15% of the mass. olefins, and even more preferably at least 20% of the mass. olefins. Since the degree of decrease in the selectivity of the middle distillate becomes large when the olefin content is 10% of the mass. or more, the effect of the present invention to maintain the selectivity of the middle distillate is even more pronounced when such a paraffin is hydrocracked.

The paraffin is not particularly limited with respect to the number of carbon atoms in it, and may be a paraffin containing hydrocarbon, which has at least 20 carbon atoms, and is preferably paraffin containing hydrocarbons that have about 20-80 carbon atoms. Even more preferably according to the present invention, the paraffin contains at least 80% of the mass. hydrocarbons having 20-80 carbon atoms.

In this embodiment, paraffin, preferably containing at least 75% of the mass. and more preferably at least 80% of the mass. normal paraffins having preferably at least 20 carbon atoms and more preferably 20-80 carbon atoms are fed to the hydrocracking treatment in the reaction column 10.

Paraffin is a paraffin that contains olefins, but is not particularly limited in other respects, and various types of oil-based paraffins and synthetic paraffins can be used as feedstock. An example of a particularly preferred paraffin is the so-called Fischer-Tropsch paraffin (FT paraffin) produced by Fischer-Tropsch synthesis (FT synthesis).

FT paraffin produced by FT synthesis and containing at least 80% of the mass. hydrocarbons having at least twenty carbon atoms may contain 20% of the mass. or more olefins, depending on differences, for example, in the type of catalyst and the reaction conditions used for the synthesis. It is particularly difficult to maintain the selectivity of the middle distillate from decreasing when such paraffin is hydrocracked, but the method of hydrocracking the paraffin of the present invention is able to satisfactorily maintain the selectivity of the middle distillate.

The catalyst contained in the first catalyst bed 12 is a catalyst that is substantially devoid of acid functionality, but is not particularly limited in other respects. This catalyst may be, for example, a catalyst in which a metal belonging to group VIII of the Periodic Table is deposited as an active metal on a support that contains at least one oxide selected from the group consisting of silica, alumina, dioxide zirconium.

Group VIII metal is cobalt, nickel, rhodium, palladium, iridium and platinum. Nickel, rhodium, palladium, iridium and platinum are preferred among them, while nickel, palladium and platinum are more preferred. These metals can be used individually or two more of them can be used in combination.

These metals may be applied to the aforementioned carrier by conventional methods, such as impregnation or ion exchange. The amount of deposited metal is preferably from 0.001 to 0.050% of the mass. relative to the carrier and more preferably from 0.005 to 0.010% of the mass. relative to the carrier. When this amount of supported metal is less than 0.001% by mass, the reaction column tends to increase strongly, and the economic performance of the process tends to decrease due to the increase in the amount of catalyst required to obtain a satisfactory retention of the selectivity of the middle distillate. On the other hand, when this amount of deposited metal exceeds 0.050% by mass, the amount of metal used becomes redundant with respect to the final deterrent effect on the selectivity of the middle distillate, and a tendency to lower economic performance of the process is added.

The catalyst contained in the second catalyst layer 14 is a catalyst that has hydrocracking activity and can be, for example, a catalyst in which a Group VIII metal of the Periodic Table is deposited as an active metal on a support comprising solid acid. In addition to its hydrocracking activity, the catalyst contained in the second catalyst bed 14 may also have hydroisomerization activity. Cracking refers to a chemical reaction that is accompanied by a decrease in molecular weight, while isomerization refers to the conversion to another compound with a different carbon skeleton, while the molecular weight and the number of carbon atoms that make up the molecule remain unchanged.

The solid acid contained in the carrier can be ultra-stable Y-type zeolite (USY), mordenite, β-zeolite, ferrierite, SSZ-22, aluminosilicate phosphate, aluminosilicate, aluminoborate, zirconium silicate. The presence of USY zeolite in the carrier is preferably among them. USY zeolite is a Y-type zeolite that becomes ultra-stable during hydrothermal treatment and / or acid treatment when new pores are formed in the range of 20-100 Ǻ in addition to the microporous structure known as micropores no more than 20 Ǻ that are initially present in Y-type zeolite. There is no particular limitation on the average particle size of the USY zeolite when used for a carrier, but preferably not more than 1.0 μm and more preferably not more than 0.5 μm. The molar ratio of silica / alumina in the USY zeolite (molar ratio of silica to alumina; hereinafter referred to as the "silica / alumina ratio") is preferably 25-120 and more preferably 30-60. The use of a USY zeolite having an average particle size of not more than 0.5 μm and a silica / alumina ratio of at least 30 is particularly preferred.

An even more suitable carrier in the present embodiment comprises a USY zeolite and at least one solid acid selected from the group of aluminosilicate, aluminoborate and zirconium silicate. Among them, a carrier containing USY zeolite and aluminosilicate is particularly preferred.

The catalyst carrier may be formed by molding a mixture that contains the aforementioned solid acid and a binder component. The binder component is not particularly limited, but alumina, silica, aluminosilicate, titanium dioxide and magnesium oxide are preferred, and alumina is more preferred.

Group VIII metal is cobalt, nickel, rhodium, palladium, iridium and platinum, where, nickel, rhodium, palladium, iridium and platinum are preferred among them, and palladium and platinum are more preferred. These metals may be used individually or two or more may be used in combination.

These metals can be applied to the aforementioned carrier by conventional methods, such as impregnation or ion exchange.

The volume of the first catalyst layer and the volume of the second catalyst layer are not particularly limited, however, the ratio of the volume VI of the first catalyst layer to the volume V2 of the second catalyst layer, or [V1 / V2] is preferably set in the present invention at 1 / 20-1 / 4. Ensuring the selectivity of the middle distillate becomes unsatisfactory when this ratio is less than 1/20. If this ratio is more than 1/4, the resulting retention effect of the selectivity of the middle distillate becomes relatively small in relation to the amount of catalyst used, and a tendency to decrease the economic performance of the process is added.

In those cases where the cross-sectional area for the cross-section on the plane perpendicular to the flow direction, the first catalyst layer and the second catalyst layer present in the reaction column 10 is constant, regardless of the cross-section position, the ratio of the thickness D1 of the first catalyst layer is 12 to the thickness D2 of the second catalyst layer 14, as shown in Figure 1, or [D1 / D2] is preferably set to a limit of 1 / 20-1 / 4.

Hydrocracking of paraffin in the reaction column 10 may be carried out under reaction conditions, such as the following. The partial pressure of hydrogen is preferably 1-12 MPa and more preferably 2-6 MPa. The hourly space velocity of the liquid (LSS) of paraffin is preferred 0.2-5.0 h ^-1 and even more preferred is 0.5-3.0 h ^-1 . The hydrogen / oil ratio (LHSV) of paraffin is preferably 0.2-5.0 h ^-1 and even more preferably 0.5-3.0 h ^-1 . The hydrogen / oil ratio is preferably 200-850 NL / L, and more preferably 350-650 NL / L.

In this description, “COSG (fluid hourly space velocity)” means the volumetric flow rate of a crude oil product (olefin-containing paraffin) under standard conditions (25 ° C, 101325 Pa) per volume of the catalyst layer in which the catalyst is packed, and the unit “h ^{- 1} "is the return hour. “NL”, that is, the unit for the volume of hydrogen in the ratio hydrogen / oil is the volume of hydrogen (L) under normal conditions (0 ° C, 101325 Pa).

The preferred hydrocracking temperature is 160-350 ° C. And more preferably 200-330 ° C.

Although paraffin is used as a downward stream in the reaction column 10 shown in Figure 1, it can, if necessary, also be used as an upward flow by changing the sequence of the first catalyst layer 12 and the second catalyst layer 14. In this case, paraffin, which passed through hydrocracking treatment, delivered from the top of the reaction column 10 to the distillation column 20.

Well-known distillation columns can be used as distillation column 20. Paraffin that passes through reaction column 10 (hydrocracking product) can be separated in distillation column 20 into desired fractions, such as, for example, naphtha (fraction with a boiling point up to 145 ° C), a kerosene fraction (fraction with a boiling point of 145-260 ° C), a gas oil fraction (fraction with a boiling point of 260-360 ° C), and a paraffin fraction (fraction with a boiling point above 360 ° C). The naphtha, kerosene and gas oil fractions used as fuel base components can, for example, be removed via lines L4-L6, connected to the distillation column 20, for example.

The liquid petroleum product manufacturing device 100 described above, due to the fact that it is equipped with a reaction column 10 that implements a method for hydrocracking paraffin, can maintain the selectivity of the middle distillate at high levels, even during hydrocracking of an olefin-containing paraffin, and can, as a result, produce components applicable as fuel base components (in particular, the middle distillate fraction encompassing the kerosene fraction and the gas oil fraction) with good yields.

In this embodiment, the paraffin that passes through the reaction column 10 (hydrocracking product) can be fed to a distillation column 20, for example, after it is separated in a gas-liquid separator into liquid petroleum products, including hydrocarbons having 5 or more carbon atoms, and unreacted hydrogen gas and light hydrocarbon gas, including hydrocarbons having no more than 4 carbon atoms.

The flow chart of FIG. 2 shows another example of a liquid petroleum product (fuel base component) manufacturing apparatus that implements the paraffin hydrocracking method of the present invention. The liquid oil production device 110 shown in FIG. 2 has the same structure as the liquid oil production device 100, except that the reaction column 10 in the liquid oil production device 100 is replaced by two reaction columns 30 and 40, which sequentially connected to each other through the transport line L7. The reaction column 30 in the liquid petroleum product manufacturing device 110 is provided with a catalyst bed 16, which is the same as the first catalyst bed described above; the reaction column 40 in the liquid oil production device 110 is provided with a catalyst bed 18, which is the same as the second catalyst bed described above; and the paraffin hydrocracking method of the present invention is carried out by these two reaction columns 30 and 40.

Hydrocracking in the reaction column 30 and the reaction column 40 may be carried out under the following reaction conditions. The partial pressure of hydrogen is preferably 1-12 MPa and more preferably 2-6 MPa. The hourly space velocity of the liquid (LSS) of paraffin is preferred 0.2-5.0 h ^-1 and more preferred, 0.5-3.0 h ^-1 . The hydrogen / oil ratio is preferably 200-850 NL / L and more preferably 350-650 NL / L. The reaction temperature of hydrocracking is preferably 160-350 ° C. And more preferred 200-330 ° C.

The catalyst contained in the catalyst bed 16 may be a catalyst substantially free of the acid functionality described previously. The catalyst contained in the catalyst bed 18 may be a catalyst having a hydrocracking activity as described above.

Neither the volume of the catalyst layer 16 in the reaction column 30 nor the volume of the catalyst layer 18 in the reaction column 40 is particularly limited, however, the ratio of the volume V3 of the catalyst layer 16 to the volume V4 of the catalyst layer 18, or [V3 / V4] is preferably set at 1/20 -1/4. In addition, in cases where the cross-sectional area for the cross-section on the plane perpendicular to the flow direction of the first catalyst layer 16 and the second catalyst layer 18 is constant, regardless of the cross-sectional position, the ratio of the thickness D3 of the catalyst layer 16 to the thickness D4 of the catalyst layer 18 shown in Figure 2, or [D3 / D4] is preferably set to a limit of 1 / 20-1 / 4.

Examples

The present invention is described in further detail by the examples below, but the present invention is not limited to these examples.

Catalyst Preparation

Catalyst 1

USY zeolite (molar ratio of silica / alumina: 40) with an average particle size of 0.4 μm, aluminosilicate (alumina content = 14 wt%) and alumina binder component as a binder were mixed / kneaded at a weight ratio of 3: 57:40 and this mixture was molded into cylinders with a diameter of 1.5 mm and a length of about 3 mm to obtain a carrier. This support was impregnated with an aqueous solution of platinum chloride in order to deposit platinum on it. It was dried for 3 hours at 120 ° C and then calcined for 1 hour at 500 ° C to obtain catalyst 1. The amount of platinum deposited was 0.8% by weight. relative to the carrier.

Catalyst 2

An alumina support with an average pore size of 100 °, molded into cylinders with a diameter of 1.5 mm and a length of about 3 mm, was impregnated with an aqueous solution of nickel nitrate to deposit nickel on it. It was dried for 3 hours at 120 ° C and then fired for 1 hour at 500 ° C to obtain catalyst 2. The amount of deposited Nickel was 0.007% of the mass. relative to the carrier.

Catalyst 3

An alumina support with an average pore size of 100 °, molded into cylinders with a diameter of 1.5 mm and a length of about 3 mm, was impregnated with an aqueous solution of platinum chloride to deposit platinum on it. It was dried for 3 hours at 120 ° C and then fired for 1 hour at 500 ° C to obtain catalyst 3. The amount of platinum deposited was 0.005% by weight. relative to the carrier.

Hydrocracking olefin-containing paraffin

Example 1

15 ml of catalyst 2 was placed on the inlet side (upper layer) of the fixed-bed reactor and 100 ml of catalyst 1 was placed on the output side (lower layer) of the fixed-bed reactor to establish a two-layer catalyst layer in the reactor. Reduction treatment was carried out for 4 hours at 345 ° C, during the introduction of hydrogen into the reactor.

After the recovery treatment, FT paraffin (C _20-81 hydrocarbon content: 95% by mass, normal paraffin content: 78% by mass, olefin content: 16% by mass) was fed as feed at a speed of 200 ml / h from the top (top side layer of the catalyst layer) of the reactor, and paraffin was hydrocracked under the reaction conditions described below in a stream of hydrogen.

In other words, hydrogen was supplied from the top of the column at a hydrogen / oil product ratio of 590 NL / L with respect to FT paraffin, and the reaction temperature was controlled at a hydrogen partial pressure of 4 MPa so as to cause a cracking rate as defined in equation (1) below up to 80% of the mass. The reaction temperature at this point was 315 ° C.

Cracking rate (% wt.) = (Mass of fraction with boiling point up to 360 ° С) / (total mass of final oil product and gaseous product) × 100 (1).

The cracking rate was calculated based on the results of gas chromatographic measurements of the hydrocracking product (final oil product and gaseous product) of FT paraffin.

The final oil product produced by hydrocracking this paraffin was distilled to obtain a middle distillate with a boiling point of 145 to 360 ° C. The yield of the middle distillate (% wt.) Relative to the FT raw paraffin and the selectivity of the middle distillate (% wt.) Were determined by the obtained middle distillate. The results are shown in Table 1. The selectivity of the middle distillate shows the proportion (% wt.) Of the middle distillate with a boiling point of 145-360 ° C. in the fraction with a boiling point up to 360 ° C. obtained under the hydrocracking conditions described above.

Example 2

Hydrocracking of paraffin was carried out as in Example 1, but in this case 10 ml of catalyst 3 was placed instead of catalyst 2 on the inlet side (top layer) of the fixed-bed reactor used in Example 1. There was no regulation of the reaction temperature based on the cracking rate, and hydrocracking was carried out at the same reaction temperature as in Example 1. The cracking rate at this time was 79%.

The middle distillate, therefore, was obtained as in Example 1, and the selectivity of the middle distillate and the yield of middle distillate were determined. The results are shown in Table 1.

Comparative Example 1

Hydrocracking of paraffin was carried out as in Example 1, but in this case, without placing catalyst 2 on the inlet side (upper layer) of the fixed-bed reactor used in Example 1. The reaction temperature, based on the cracking rate, was not controlled, and hydrocracking was carried out at the same reaction temperature as in Example 1. The cracking rate at this time was 84%.

The middle distillate, therefore, was obtained as in Example 1, and the selectivity of the middle distillate and the yield of middle distillate were determined. The results are shown in Table 1.

Table 1 Example 1 Example 2 Comparative Example 1 The output of the middle distillate (% wt.) 63,4 63.1 52.1 The selectivity of the middle distillate (% wt.) 79 80 62

As shown in Table 1, the paraffin hydrocracking method of Examples 1 and 2, in which paraffin was passed in sequence through a catalyst bed lacking acid functionality, and then through a catalyst bed having hydrocracking activity, was shown to have the ability, even when the paraffin contained high olefin concentration, maintain a sufficiently high selectivity of the middle distillate and obtain a middle distillate with sufficient yield.

Industrial applicability

The present invention provides a method for paraffin hydrocracking, which allows maintaining the selectivity of the middle distillate at high levels during hydrocracking of an olefin-containing paraffin. The present invention provides a method for producing fuel base components that uses this hydrocracking method.

Claims (4)

1. The method of paraffin hydrocracking consists in passing an olefin-containing paraffin obtained by Fischer-Tropsch synthesis in the presence of hydrogen and in a predetermined sequence through a first catalyst bed that contains a catalyst substantially lacking acid functionality, which includes a support and a Group VIII metal supported on the specified carrier, and the applied amount of this metal is equal to 0.005-0.010 wt.% relative to the specified carrier, and a second catalyst layer that contains a catalyst having an asset the ability to hydrocracking and including a metal of group VIII deposited on a carrier comprising solid acid. 2. The method of paraffin hydrocracking according to claim 1, characterized in that the carrier contains at least one of the oxides selected from the group consisting of silicon dioxide, aluminum oxide and zirconia. 3. The method of hydrocracking paraffin according to any one of claims 1 and 2, characterized in that the support of the catalyst contained in the second catalyst bed comprises ultra-stable Y-type zeolite. 4. A method of obtaining a fuel base component, characterized by fractional distillation of a hydrocracking product obtained by the method of hydrocracking paraffin according to any one of claims 1 to 3 to obtain a fuel base component.

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