RU2575172C1 - Catalyst for combined obtaining of waxy fuels and isoparaffin oils and method for combined obtaining of waxy fuels and isoparaffin oils in process of isomerisation/cracking of high-paraffin raw material with application thereof - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: catalyst contains zeolite SAPO-41 or MgAPSO-41, which has acidity, determined by ammonia TPD method, 0.30-0.75 mmol/g with the following component content, wt %: platinum 0.1-0.5; zeolite SAPO-41 or MgAPSO-41, which has acidity, determined by ammonia TPD method, 0.30-0.75 mmol/g 20.0-80.0; aluminium oxide - the remaining part. In order to realise combined obtaining of waxy jet or Diesel fuel and isoparaffin oil process of isomerisation/cracking of high-paraffin raw material is carried out in flow mode with contact of flow of gas-liquid mixture, consisting of high-paraffin raw material and hydrogen, with immobile layer of above said catalyst at temperature 380-440°C, pressure 2.0-4.0 MPa, volume rate of raw material supply 1.0-1.5 h^-1, hydrogen/raw material ratio 1000:1 nl/l. after separation of hydrogen-containing gas obtained total product of isomerisation/cracking process is divided with separation of target products or is subjected to hydrofinishing and further separation with isolation of target products.

EFFECT: increase of output and quality of waxy Diesel or jet fuel and isoparaffin oil from crude oil or synthetic high-paraffin raw material.

4 cl, 5 tbl, 8 ex

Description

The invention relates to the field of catalysis and oil refining, in particular to the composition of a catalyst based on aluminophosphate zeolite having an AFO structure, providing the joint production of low-curing diesel or jet fuels and isoparaffin oils from high-paraffin raw materials.

High-paraffin feed means a mixture of hydrocarbons, which consists of more than 90 wt.% Paraffins and contains hydrocarbons with more than 16 carbon atoms. Moreover, most of the paraffins have an unbranched structure. High paraffin raw materials include both products isolated from oil oil fractions - gachi, paraffins, ceresins and petrolatums, as well as synthetic solid hydrocarbons (STU) obtained from CO and H ₂ by the Fischer - Tropsch synthesis. To obtain fuels and oils from these types of highly paraffin raw materials, their hydrocatalytic processing is necessary, during which hydroisomerization and hydrocracking reactions are targeted. In the description and examples of the present invention, a process aimed at the joint production of fuels and isoparaffin base oils from high-paraffin raw materials, during which hydroisomerization and hydrocracking reactions are targeted, is termed isomerization / hydrocracking.

From literature data, it is known that bifunctional catalysts based on aluminophosphate zeolites of a specific structure — AEL (for example, SAPO-11, MeAPO-11, MeAPSO-11), ATO (for example, SAPO-31, MeAPO-, show high selectivity in the hydroisomerization reactions of long chain paraffins 31, MeAPSO-31) and AFO (e.g., SAPO-41, MeAPO-41, MeAPSO-41). Such zeolites have a one-dimensional pore system and ten-membered or small twelve-membered rings at the mouths of channels that do not have large cavities, and can be assigned to the group of so-called 1-D, 10-R molecular sieves.

Bifunctional catalysts based on the aluminophosphate zeolites of the indicated types containing a metal component active in hydrogenation-dehydrogenation reactions are characterized by higher selectivity with respect to hydroisomerization reactions in comparison with catalysts based on such common zeolites as Y, β, ZSM-5, as well as catalysts based on amorphous aluminosilicates and halogenated aluminum oxide. Deldari N. Suitable catalysts for hydroisomerization of long-chain normal paraffins. Applied Catalysis A. 2005, v. 293, p. 1-10. Akhmedov V.M. Al-Khowaiter S.H. Recent advances and future aspects in the selective isomerization of high n-alkanes. Catalysis Reviews. 2007, v. 49, p. 33-139.

The known composition and method of producing a catalyst based on a molecular sieve, which is a mixture of zeolites with the structure of AEL (SAPO-11) and AFO (SAPO-41) and at least 5 wt.% Amorph. The catalyst containing 0.5 wt.% Pt on a support consisting of 70 wt.% Of the indicated molecular sieve and 30 wt.% Alumina showed high activity and selectivity in the hexadecane hydroisomerization reaction (selectivity up to 98%, hydroisomerization yield up to 83 %). US 2010/0317910 A1, December 16, 2010.

A method for synthesizing zeolite with the AEL structure (SAPO-11) is also known, the diffraction pattern of which remains practically unchanged after calcining the zeolite to remove the template. The catalyst based on synthesized SAPO-11 contains 10-85 wt.% Zeolite and 0.05-1.5 wt.% Pd or Pt, the rest is aluminum oxide. The catalyst was characterized by increased selectivity (up to 90%) with respect to hydroisomerization reactions of long chain n-paraffins. It should be noted that the tested catalyst did not provide high yields during hydroisomerization of a fraction of 350-545 ° C isolated from vacuum gas oil hydrocracking products and having a pour point of 30 ° C and a viscosity index of 125. Under the following process conditions: temperature 360 ° C, pressure 5.0 MPa, a volumetric feed rate of 1.5 h ^-1 , a product with a pour point of minus 16 ° C, having a viscosity index of 120, was obtained with a yield of 84.2 wt.%. US 6,596,156 B1, 04/22/2003.

Since catalysts based on aluminophosphate zeolites of the AEL, ATO, and AFO structures exhibit high selectivity with respect to hydroisomerization reactions of long-chain paraffins, they were proposed for the production of fuels and oils from various types of high-paraffin feedstocks and made it possible to obtain higher yields of products with better low-temperature characteristics Compared to classic bifunctional catalysts.

So, when using a high-paraffin feed (oil-free oil) in the process of catalytic isomerization of a highly porous catalyst with a high surface area, which is an active metal of group VIII, for example, platinum on fluorinated metal oxide - gamma or eta-alumina, which has a pore volume of at least 0 , 50 cm ³ / g and a specific surface area of at least 140 m ² / g, the specified catalyst did not provide the necessary low-temperature characteristics of the resulting base oil. The isolated oil fraction of 390 ° C ^{+ was} further subjected to solvent dewaxing to obtain a product having a pour point of about minus 20 ° C. EP 0 585 358 B1, 09/10/1997.

This problem is solved by processing high-paraffin raw materials using catalysts based on 1-D, 10-R molecular sieves.

Thus, the hydroisomerization process of high-paraffin raw materials is known to produce low-hardening base oils, characterized by the use of relatively low pressures (0.7-2.8 MPa) and layer-by-layer loading of at least two types of catalysts based on 1-D, 10-R molecular sieves into the hydroisomerization reactor . Preferred for use in the first catalyst is a zeolite with an AEL structure (SAPO-11 or SM-3), in the second catalyst, a zeolite with an MTT structure (ZSM-23 or SSZ-32). Catalyst carriers also contain alumina. As the active metal of the catalysts, platinum and palladium are preferred. As the raw material of the hydroisomerization process, STUs obtained by the Fischer – Tropsch synthesis and subjected to the hydrogenation process were used. During the layer-by-layer loading of catalysts (the first catalyst contained platinum on a support consisting of 85 wt.% SM-3 and 15 wt.% Alumina; the second catalyst contained platinum on a support consisting of 65 wt.% SSZ-32 and 35 wt.% alumina) and the following process conditions: the volumetric feed rate of 1.0 h ^-1 , the ratio of hydrogen to feed 886 nm ³ / m ³ , the resulting isomerized product having a pour point of minus 28 ° C and containing 49 wt.% oil fraction 371-566 ° C. In this case, the process feed contained about 70 wt.% Of the fraction 371-566 ° C. US 7384538 B2, 06/10/2008.

Also known is a catalyst based on aluminophosphate zeolite of the SAPO type having the AEL structure (SM-7), which was used in the hydroisomerization of STUs obtained by Fischer-Tropsch synthesis and subjected to hydrogenation. Silicon “domains” distributed in the bulk of SM-7 zeolite ensured high selectivity of catalysts based on it in the process of catalytic hydroisomerization of highly paraffin feed. The catalyst containing 0.4 wt.% Pt on SM-7 was tested in the process of hydroisomerization of STU obtained by Fischer-Tropsch synthesis and subjected to hydrogenation under the following process conditions: pressure 2.1 MPa, feed volumetric rate 0, 85 h ^-1 , the ratio of hydrogen to feed 886 nm ³ / m ³ . The hydroisomerization temperature was set so that the 343 ° C ⁺ fraction extracted from the total product had a pour point of minus 28 ° C. The Pt / SM-7 catalyst provided an oil fraction of 343 ° C ⁺ having a viscosity index of 155 about 68% by weight. At the same time, the process feed contained about 80 wt.% Of the 343 ° C ⁺ fraction. US 2010/0029998 A1, December 16, 2010.

The disadvantage of these methods can be considered the fact that before processing in the process of hydroisomerization, the STUs obtained by the Fischer-Tropsch synthesis must be hydrogenated.

Known dewaxing catalyst containing aluminophosphate zeolite structure AEL (SAPO-11), alumina, as well as platinum or palladium. The catalytic dewaxing process using this catalyst is described in the method for producing low-curing diesel fuels and oils from Fischer-Tropsch synthesis products. So, in the catalytic dewaxing of C ₅ ⁺ hydrocarbons obtained by Fischer-Tropsch synthesis on a catalyst containing platinum and 25 wt.% SAPO-11, alumina - the rest, under the following conditions: 6.9 MPa, bulk feed rate 1, 0 h ^-1 , the ratio of hydrogen to feed 1773 nm ³ / m ³ , obtained 64% of the diesel fraction 149-371 ° C, having a cloud point of minus 35 ° C and 16% of the oil fraction 371 ° C ⁺ , having a pour point minus 12 ° C. In this case, the process feed contained about 60% of the fraction 149-371 ° C and about 30% of the oil fraction 371 ° C ⁺ . US 6702937 B2, 03/09/2004.

The disadvantages of this method include the relatively low yield of diesel fraction.

Closest to the proposed catalyst for the isomerization / hydrocracking of high paraffin feed is a catalyst for the stage of hydrocracking / isodeparaffinization containing a carrier made from a mixture of 10-40 wt.% Zeolite SAPO-41 and 60-90 wt.% Al ₂ O ₃ and platinum in the range 0.2-0.4 wt.%. The method of producing diesel fuel includes hydrocracking / isodeparaffinization of solid hydrocarbons on the above catalyst on a stationary catalyst bed at a pressure of 1-6 MPa, a temperature of 340-420 ° C, a hydrocarbon feed rate of 0.5-1.5 h ^-1 , the ratio of hydrogen: hydrocarbons 800-1200: 1 nl / l, followed by isolation by fractionation from hydrocracking products of a fraction of 180-360 ° C, which is subjected to hydrofinishing. Synthetic solid hydrocarbons (STU) obtained by the Fischer-Tropsch method are used as feedstock. RU 2493237, 09/20/2013.

The technical task of the invention is to develop a catalyst that allows to jointly obtain low-curing diesel or jet fuels and isoparaffin base oils, and a method for their production in the isomerization / hydrocracking of high-paraffin raw materials.

The technical result from the implementation of the claimed group of inventions is to ensure high yield and quality of low-setting diesel or jet fuel and isoparaffin oil from high-paraffin oil.

The technical problem is solved in that the catalyst for the joint production of low-hardening diesel or jet fuels and isoparaffin base oils contains an SAPO-41 or MgAPSO-41 zeolite having an acidity determined by the ammonia TPD method of 0.30-0.75 mmol / g in the following the content of components, wt.%:

platinum 0.1-0.5 zeolite SAPO-41 or MgAPSO-41 having acidity, determined by the TPD method of ammonia, 0.30-0.75 mmol / g 20.0-80.0 aluminium oxide rest

In accordance with the task, a method has been developed for the joint production of low-curing diesel or jet fuels and isoparaffin oils in the isomerization / hydrocracking of high-paraffin raw materials using the claimed catalyst.

The method for the joint production of low-curing diesel or jet fuels and isoparaffin base oils in the isomerization / hydrocracking process of high-paraffin feed using the above catalyst is characterized in that the isomerization / hydrocracking process is carried out in a flow mode when the gas-liquid mixture consisting of petroleum paraffin and hydrogen is in contact with a stationary a catalyst layer at a temperature of 380-440 ° C, a pressure of 2.0-4.0 MPa, a volumetric feed rate of 1.0-1.5 h ^-1 , the ratio of water genus / raw material 1000: 1 nl / l. After separation of the hydrogen-containing gas, the total product is separated with the release of the target products or subjected to hydrofinishing and subsequent separation with the release of the target products.

The method is as follows.

To prepare the catalyst, a support is synthesized containing aluminophosphate zeolite SAPO-41 or MgAPSO-41, having an acidity determined by the TPD method of ammonia, 0.30-0.75 mmol / g and alumina. Platinum is applied to the carrier obtained. The finished catalyst contains: 0.1-0.5 wt.% Pt, 20-80 wt.% Aluminophosphate zeolite structure AFO having an acidity determined by the method of TPD ammonia, 0.30-0.75 mmol / g, alumina - rest.

The resulting catalyst is used for the joint production of low-setting jet or diesel fuel and isoparaffin oil. For this purpose, high-paraffin feed - oil-derived paraffin - is sent to an isomerization / hydrocracking reactor, into which an catalyst based on aluminophosphate zeolite of the AFO structure having an acidity of 0.30-0.75 mmol / g determined by the TPD method of ammonia is loaded. The isomerization / hydrocracking process is carried out at a temperature of 380-440 ° C, a pressure of 2.0-4.0 MPa, a volumetric feed rate of 1.0-1.5 h ^-1 , a hydrogen / feed ratio of 1000: 1 nl / L. After separation of the hydrogen-containing gas, the total product is separated with the release of the target products or subjected to hydrofinishing and subsequent separation with the release of the target products.

The invention is illustrated, but not limited to, by the following examples.

Example 1

To prepare catalyst No. 1, SAPO-41 zeolite was used as the main acid component, the number of acid sites on the surface of which (acidity) was 0.57 mmol / g. The zeolite acidity was measured by the method of thermally programmed desorption (TPD) of ammonia using the following procedure. The analysis is carried out in a laboratory setup with a constant helium current of 30 cm ³ / min. 0.200 g of the powdery sample is placed on a substrate of porous quartz material in a cell that is a hollow quartz tube. The sample is heated to a temperature of 550 ° C and kept at this temperature for 1.5 hours. Then the temperature is lowered to 100 ° C and the sample is treated with a mixture of helium and ammonia (NH3 content of 2.5 vol%) until the surface of the sample is saturated with ammonia. Physically sorbed ammonia is blown off at the same temperature and increased helium flow (150 cm ³ / min) for 1 h. The temperature of the sample is reduced to room temperature. The TPD spectrum is taken when the temperature of the sample rises at a rate of 5 ° C / min to 550 ° C. The signal is recorded using a thermal conductivity detector. To determine the number of acid sites on the sample surface, the thermal conductivity detector was calibrated using mixtures of helium and ammonia of known concentration.

Preparation of catalyst No. 1 includes the following steps:

1. In a porcelain mortar, 44.4 g of zeolite powder and 79.1 g of pseudoboehmite are mixed and ground with a pestle until smooth.

2. 90 ml of a solution consisting of 80.8 ml of distilled water, 2.5 ml of nitric acid and 6.7 ml of triethylene glycol are poured into the resulting mixture in small portions. The resulting mass is mixed until a homogeneous paste.

3. The resulting paste is formed using a laboratory piston extruder with a 1.5 mm die.

4. The resulting extrudates are dried at room temperature for 15 hours, dried by stepwise raising the temperature (60, 80, 110 ° C) and holding at each temperature for 2 hours, and then crushed to granules with a length of 1.5-2.5 mm

5. The obtained granules are calcined at a temperature of 550 ° C in a stream of air for 10 hours

6. Prepare 250 ml of an impregnating solution, for the preparation of which 222.3 ml of distilled water, 25.1 ml of a solution of H ₂ PtCl _{6 with a} concentration of 12 mg Pt / ml, 1.2 ml of concentrated hydrochloric acid and 1.4 ml of “glacial” are mixed acetic acid.

7. The calcined carrier is poured with an impregnating solution and kept at room temperature for 16 hours.

8. After the end of the impregnation step, the impregnation solution is decanted, and the catalyst is dried by stepwise raising the temperature (60, 80, 110 ° C) and holding at each temperature for 2 hours.

Example 2

Catalyst No. 2 was synthesized similarly to catalyst No. 1, the preparation of which is described in Example 1, except that instead of the alumophosphate zeolite SAPO-41 having an acidity determined by the ammonia TPD method of 0.57 mmol / g, MgAPSO-41 zeolite was used having an acidity determined by the TPA method of ammonia, 0.75 mmol / g.

Example 3

For the synthesis of catalyst No. 3, SAPO-41 zeolite is used, having an acidity determined by the ammonia TPD method of 0.30 mmol / g.

Preparation of catalyst No. 3 includes the following stages:

1. In a porcelain mortar, 88.9 g of zeolite powder and 26.4 g of pseudoboehmite are mixed and ground with a pestle until smooth.

2. 80 ml of a solution consisting of 72.1 ml of distilled water, 0.9 ml of nitric acid and 7.0 ml of triethylene glycol are poured into the resulting mixture in small portions. The resulting mass is stirred until a homogeneous paste and evaporated to remove excess moisture.

3. The resulting paste is formed using a laboratory piston extruder with a 1.5 mm die.

4. The resulting extrudates are dried at room temperature for 15 hours, dried by stepwise raising the temperature (60, 80, 110 ° C) and holding at each temperature for 2 hours, and then crushed to granules with a length of 1.5-2.5 mm

5. The obtained granules are calcined at a temperature of 550 ° C in a stream of air for 10 hours

6. The calcined support is poured into 250 ml of a solution of Pt (NH ₃ ) ₄ Cl _{2 at a} concentration of 2 mg Pt / ml and incubated at 95 ° C for 7 hours.

7. After the end of the platinum deposition step, the impregnation solution is decanted, and the catalyst is dried by a stepwise increase in temperature (60, 80, 110 ° C) and exposure at each temperature for 2 hours.

8. After the drying step, the catalyst is calcined by raising the temperature to 500 ° C at a rate of 20 ° C / h and holding at this temperature for 3 hours

Example 4

For the synthesis of catalyst No. 4, MgAPSO-41 zeolite is used having an acidity of 0.75 mmol / g determined by the TPD method of ammonia.

Preparation of catalyst No. 4 includes the following stages:

1. In a porcelain mortar, 22.2 g of zeolite powder and 105.4 g of pseudoboehmite are mixed and ground with a pestle until smooth.

2. 95 ml of a solution consisting of 84.7 ml of distilled water, 3.4 ml of nitric acid and 6.9 ml of triethylene glycol are poured into the resulting mixture in small portions. The resulting mass is mixed until a homogeneous paste.

3. The resulting paste is formed using a laboratory piston extruder with a 1.5 mm die.

4. The resulting extrudates are dried at room temperature for 15 hours, dried by stepwise raising the temperature (60, 80, 110 ° C) and holding at each temperature for 2 hours, and then crushed to granules with a length of 1.5-2.5 mm

5. The obtained granules are calcined at a temperature of 550 ° C in a stream of air for 10 hours

6. Prepare 250 ml of an impregnation solution, for the preparation of which 240.8 ml of distilled water, 8.3 ml of a solution of H ₂ PtCl _{6 with a} concentration of 12 mg Pt / ml, 0.4 ml of concentrated hydrochloric acid and 0.5 ml of “glacial” are mixed acetic acid.

7. The calcined carrier is poured with an impregnating solution and kept at room temperature for 17 hours.

8. After the end of the impregnation step, the impregnation solution is decanted, and the catalyst is dried by stepwise raising the temperature (60, 80, 110 ° C) and holding at each temperature for 2 hours.

Example 5

Catalyst No. 5 is synthesized in a similar manner to catalyst No. 1, the preparation of which is described in Example 1, except that instead of the alumophosphate zeolite SAPO-41 having an acidity determined by the ammonia TPD method of 0.57 mmol / g, MgAPSO-41 zeolite was used having an acidity determined by the TPA method of ammonia, 0.50 mmol / g.

Example 6

Comparison catalyst No. 1 is synthesized in the same way as catalyst No. 1, the preparation of which is described in Example 1, except that instead of the aluminophosphate zeolite SAPO-41 having an acidity determined by the ammonia TPD method of 0.57 mmol / g, SAPO- zeolite was used 41 having an acidity determined by the TPA method of ammonia of 0.11 mmol / g.

Example 7

Comparison catalyst No. 2 is synthesized in the same way as catalyst No. 1, the preparation of which is described in Example 1, except that instead of the aluminophosphate zeolite SAPO-41 having an acidity determined by the ammonia TPD method of 0.57 mmol / g, MgAPSO- zeolite was used 41 having an acidity determined by the TPA method of ammonia of 0.95 mmol / g.

The composition of the synthesized catalysts is presented in table 1.

Example 8

Catalysts No. 1-5, as well as comparative catalysts No. 1-2, synthesized according to the methods described in Examples 1-7, were tested in the process of isomerization / hydrocracking of petroleum paraffin. Used brand P-2 paraffin is a mixture of hydrocarbons with the number of carbon atoms from C ₁₉ to C ₃₆ with a predominant content of paraffins of normal structure. At the same time, paraffin practically does not contain sulfur, nitrogen and aromatic hydrocarbon compounds. Less than 0.5 vol.% P-2 brand paraffin boils up to a temperature of 360 ° C. Thus, the raw materials used can be characterized as a fraction of 360 ° C +.

The isomerization / hydrocracking process is carried out on a flow-through catalytic unit equipped with a heated casing, in which a feed tank, reactor, mixer, gas and liquid lines suitable for the reactor are placed. The heated casing allows reagents to be heated and the unit used to work with raw materials that are solid under normal conditions. The inner diameter of the reactor is 13 mm, the catalyst loading is 10 cm ³ .

Before testing, the catalyst is reduced in a stream of hydrogen according to the following temperature program:

- rise to a temperature of 250 ° C at a speed of 100 ° C / h;

- exposure at a temperature of 250 ° C for 1 h;

- rise to a temperature of 450 ° C at a speed of 50 ° C / h;

- exposure at a temperature of 450 ° C for 3 hours

During the tests, water from the tank on the balance is supplied to the system by a high pressure pump. The amount of water supplied is measured and recorded. The water pumped by the pump enters the lower part of the feed tank and displaces the high-paraffin raw materials contained in it into the mixer. In the mixer, the feed is mixed with hydrogen and fed to the reactor. Products from the bottom of the reactor pass through the product line, heated by an elastic tape electric heater, and enter the separator. In the separator, the gas phase is separated from the liquid product. Next, the liquid product enters the sampler refrigerator, where it is heated or cooled by the antifreeze pumped through the jacket of the apparatus. Periodic sampling of liquid catalysis is carried out from the refrigerator-sampler.

The isomerization / hydrocracking process is carried out under the following conditions: pressure 2.0-4.0 MPa, bulk feed rate 1.0-1.5 h ^-1 , hydrogen: feed ratio 1000: 1 nl / l.

The products obtained at various process temperatures were dispersed to isolate the NK-180 ° C, 180-360 ° C and 360 ° C-KK fractions.

The total isomerization / hydrocracking product obtained using catalyst No. 5 was sent to the hydrofinishing step, which was carried out using a catalyst representing 1 wt.% Pd on γ-Al ₂ O ₃ , under the following conditions: temperature 200 ° C, pressure 4.0 MPa, a volumetric feed rate of 10 h ^-1 , a hydrogen: feed ratio of 500: 1 nl / l. The resulting hydrofinishing product was dispersed with the allocation of fractions NK-135 ° C, 135-280 ° C and 280 ° C-KK.

The yields and characteristics of the target products - diesel (fraction 180-360 ° C) or jet fuel (fraction 135-280 ° C) and isoparaffin base oil (fraction 360 ° C-KK or 280 ° C-KK) are presented in tables 2-3 .

* for jet fuel, the density and kinematic viscosity were determined at 20 ° С; instead of the limiting filterability temperature, the temperature of the onset of crystallization was determined.

Table 4 presents the main physico-chemical characteristics of a sample of diesel fuel (fractions 180-360 ° C), obtained in the process of isomerization / hydrocracking of oil paraffin on catalyst No. 1 at a temperature of 410 ° C, a pressure of 4.0 MPa, a volumetric feed rate of 1 , 5 h ^-1 , the ratio of hydrogen to feed 1000: 1 nl / L. Under the indicated process conditions, total catalysis was obtained with a yield of 91.3 wt.%, From which a 180-360 ° C fraction was isolated with a yield of 68 vol.%. The obtained sample of diesel fuel in accordance with all the main characteristics (except density) met the requirements of GOST R 52368-2005. By such indicators as the content of polycyclic aromatic hydrocarbons and the cetane index, the resulting diesel fuel has a significantly higher quality in relation to the requirements of the regulatory document.

Table 5 presents the main physicochemical characteristics of a sample of isoparaffin base oil (fraction 360 ° С-КК) obtained during isomerization / hydrocracking on catalyst No. 1 at a temperature of 385 ° С, a pressure of 2.0 MPa, a volumetric feed rate of 1, 5 h-1, the ratio of hydrogen to feed 1000: 1 nl / L. Under the indicated process conditions, total catalysis was obtained with a yield of 96.2 wt.%, From which a 360 ° С-КК fraction was isolated with a yield of 58 vol.%. For all certain indicators, the obtained base oil can be assigned to group III + according to API classification.

Claims (4)

1. The catalyst for the joint production of low-hardening diesel or jet fuels and isoparaffin base oils containing platinum, zeolite and alumina, characterized in that it contains zeolite SAPO-41 or MgAPSO-41, having an acidity determined by the method of TPD ammonia, 0, 30-0.75 mmol / g in the following components, wt.%:
platinum 0.1-0.5 zeolite SAPO-41 or MgAPSO-41 having acidity, determined by the TPD method of ammonia, 0.30-0.75 mmol / g 20.0-80.0 aluminium oxide rest 2. A method for the joint production of low-curing diesel or jet fuels and isoparaffin base oils in the isomerization / hydrocracking process of high-paraffin feed using a catalyst according to claim 1, characterized in that the isomerization / hydrocracking process is carried out in a flow mode when the gas-liquid mixture consisting of oil is contacted paraffin and hydrogen, with a fixed catalyst bed at a temperature of 380-440 ° C, a pressure of 2.0-4.0 MPa, a volumetric feed rate of 1.0-1.5 h ^-1 , the ratio of hydrogen / raw material e 1000: 1 nl / l, hydrogen-containing gas is separated, the resulting total product of the isomerization / hydrocracking process is separated with the release of the target products or subjected to hydrofinishing and subsequent separation with the release of the target products. 3. The method according to p. 2, characterized in that the total product of the isomerization / hydrocracking process is separated with the allocation of the target products - diesel fuel and isoparaffin base oil. 4. The method according to p. 2, characterized in that the total product of the isomerization / hydrocracking process is subjected to hydrofinishing and subsequent separation with the selection of the target products - jet fuel and isoparaffin base oil.