RU2726616C1 - Method for combined hydroprocessing of vegetable and oil raw materials - Google Patents

Abstract

FIELD: technological processes.SUBSTANCE: invention relates to a method for hydrogenation treatment of vegetable and oil raw materials. Vegetal component is represented by a lipid fraction extracted from microalgae or non-edible vegetable oils, and the oil component is a straight-line diesel fraction mixed with light catalytic cracking and coking gasoil. Process of combined hydroprocessing is carried out in three stages: at the first stage the raw material consisting of straight-run diesel fraction and mixture of light gasoil of catalytic cracking and coking in ratio of 60.0–80.0:20.0–40.0 wt%, respectively, subjected to hydrotreating in presence of cobalt-molybdenum catalyst based on aluminum oxide or aluminosilicate to obtain hydrogenate with content of sulfur in range of 150–500 ppm. Further, at the second hydroprocessing step, the feedstock consisting of the first stage hydrohexate and the vegetable component in ratio of 80.0–95.0:5.0–20.0 wt%, respectively, subjected to hydrodeoxygenation combined with hydrodesulphurisation in the presence of a pack of catalysts: massive molybdenum disulphide in a first layer and a nickel-albolmolybdenum catalyst based on aluminum oxide or aluminosilicate in a second layer. At the third stage of the process, catalytic hydrodewaxing is carried out in the presence of a zeolite-containing nickel-molybdenum catalyst. Obtained product is subjected to stabilization and 180-kk °C fraction is removed as a component of diesel fuel.EFFECT: production of diesel fuel with improved low-temperature properties.4 cl, 7 ex

Description

The invention relates to the field of oil refining, in particular to the field of joint hydro-processing of vegetable and petroleum hydrocarbon raw materials in order to obtain a diesel fuel component with improved low-temperature properties.

The production of biofuels from plant raw materials is one of the intensively developing areas of research today, which is associated with the need to reduce the environmental load on the environment and the search for an alternative raw material base for the production of motor fuels.

Today, there are two methods for processing renewable raw materials: individual processing of plant components (transesterification or hydrodeoxygenation of triglycerides of fatty acids, etc.) and joint processing of oil and vegetable raw materials. The second method has a number of advantages over the first in terms of the absence of capital costs for the construction of new technological units and lower operating costs, which leads to a lower cost of the produced biofuels. The restriction on the widespread use of biomass as a component of the feedstock of a hydrotreating unit is due to the specificity of its chemical composition, namely, the high content of organo-oxygen and unsaturated compounds, which, even under mild process conditions, on the one hand, lead to the rapid deactivation of industrial catalysts [D. Kubicka, J. Nogasek // Appl. Catal. A. 2011. V. 394. P. 9-17], and, on the other hand, to inhibition by oxygen-containing compounds of target reactions of sulfur removal and hydrogenation of polycyclic aromatic hydrocarbons. Therefore, for the joint processing of fossil and renewable raw materials, it is necessary to develop an optimal technology that combines highly active stable catalytic systems and effective technological solutions.

A known method of producing diesel fuel from renewable raw materials of plant origin [RF Patent No. 2558948, 08/10/2015].

The method is carried out by one-stage hydro-processing and isomerization using raw materials of plant (biological) origin, selected from vegetable oils or microalgae lipids, in the presence of a bifunctional heterogeneous catalyst. The catalyst is a crystalline silicoaluminophosphate with a zeolite-like structure, modified with a metal of Group VIII of the Periodic Table, with a fineness of the metal introduced into the catalyst composition - 14-60%, in an amount of not more than 10 wt. %. A SAPO-31 silicoaluminophosphate catalyst is preferred. The method uses a mixture of raw materials of plant origin (fats, oils, lipids of microalgae) with hydrotreated diesel fuel. The process is carried out at a temperature not exceeding 400 ° C, a pressure not exceeding 10 MPa, a mass feed rate of the raw material not exceeding 10 h ^-1 , a hydrogen / raw material volume ratio not exceeding 2000.

EFFECT: dilution of vegetable raw materials with minerals allows to increase the stability of the bifunctional catalyst and increase its operation time.

The disadvantages of this method include the need to use hydrotreated diesel fuel for processing in a mixture with vegetable raw materials, which requires either deep hydrotreating with strict operating parameters, or does not allow a large amount of low-quality secondary gas oils to be involved in the hydrotreating feedstock.

Also known is a method of joint processing of diesel fuel and vegetable oil to obtain a hybrid diesel biofuel with a low cloud point [RF Patent No. 2487923, 09/29/2009].

The method for producing a hybrid diesel fuel product includes the following stages: combining vegetable oil with a diesel fraction to form a first mixture with a vegetable oil content of not more than 10 wt. %; hydrotreating the first mixture to form a hydrotreated second mixture containing deoxygenated triglyceride components, with a sulfur removal rate of at least 95%; isomerizing the hydrotreated second mixture in the presence of an isomerization catalyst to form a third mixture comprising a hybrid diesel fuel having a reduced cloud point.

EFFECT: no interstage removal of H ₂ S and NH ₃ is required between the stages of hydrotreating and isomerization, a hybrid diesel product with a low cloud point is formed, increasing productivity while reducing overall production costs.

The disadvantages of this method include the involvement in the process of edible plant materials with a low content of what? (up to 10% of the mass.). The disadvantages of this method also include the use of expensive catalysts based on platinum and palladium at the isomerization stage, as well as the inability to use sulfur and high-sulfur diesel fractions, since the declared degree of sulfur removal (not less than 95%) will not allow obtaining a product that meets modern specifications for residual sulfur content.

The known method and catalyst for hydroprocessing for the production of high-quality diesel and oil fuels from raw materials that contain oxygen-containing components obtained from renewable organic materials [RF Patent No. 2495082, 23.07.2009].

A method for the production of hydrocarbon fuel from renewable organic material of biological origin includes the following stages:

1. Formation of feedstock by combining fossil hydrocarbon fuels with renewable organic material, where the renewable organic material content is from 1 to 35 vol. %;

2. Mixing the feedstock from step (1) with an enriched hydrogen-containing gas and feeding the combined stream to the hydrodeoxygenation step by contacting said combined stream with a hydrodeoxygenation catalyst. In this case, the hydrodeoxygenation catalyst is a supported molybdenum catalyst with a Mo content of 0.1 to 20 wt. %, the support is selected from the series of aluminum oxide, silicon dioxide, titanium dioxide and their combinations (said support has a bimodal porous structure with pores with a diameter of more than 50 nm, which make up at least 2 vol.% of the total pore volume).

In addition, after hydrodeoxygenation, the resulting product is subjected to additional hydrotreating and hydroisomerization. Animal fats, tall oil, rapeseed oil are used as renewable organic material. The stage of hydrodeoxygenation is carried out at a hydrogen pressure of 1-200 bar (0.1-20 MPa), at a temperature of 50-350 ° C and at a volumetric feed rate of 0.1-10 h ^-1 . The stages of hydrotreating and hydroisomerization are carried out at a hydrogen pressure of 1-200 bar (0.1-20 MPa), at a temperature of 50-450 ° C and at a volumetric feed rate of 0.1-10 h ^-1 .

EFFECT: reduced tendency to form coke due to low local partial pressure of hydrogen.

The disadvantage of this method is the involvement of edible plant materials in the process. The disadvantages also include the fact that when using high-sulfur raw materials, it is not possible to obtain a product that meets modern requirements for the sulfur content.

Closest to the claimed is a method of hydrofinishing of triglycerides of fatty acids and straight-run diesel fraction on sulfide catalysts in order to obtain low-sulfur hydrocarbon fractions [RF Patent 2652991, 04/05/2018]

In accordance with the invention, the hydrofinishing of triglycerides of fatty acids in a mixture with petroleum fractions is carried out on sulfide catalysts MoS ₂ / Al ₂ O ₃ and NiMo / Al ₂ O ₃ in two stages. At the first stage, a straight-run diesel fraction is hydrotreated in the presence of a sulfide NiMo / Al ₂ O ₃ catalyst, then the resulting mixture of hydrocarbons, hydrogen and hydrogen sulfide is mixed with triglycerides of fatty acids and the hydrodeoxygenation reaction is carried out in the presence of a sulfide catalyst MoS ₂ / Al ₂ O ₃ . Hydro-refining of raw materials is carried out at a temperature of 340 ° C, a hydrogen pressure of 4.0 MPa, a volumetric flow rate of raw materials - 1.1-1.25 h ^-1 , a total volumetric ratio of hydrogen / raw materials - 510-600 Nm ³ / m ³ .

The technical result is a high efficiency of the process of combined hydrofining of diesel fractions and triglycerides of fatty acids.

The disadvantages of this method include the impossibility of expanding the resource base due to the use of high-sulfur gas oils from secondary processing processes, as well as the impossibility of obtaining low-solidifying hydrocarbon fractions.

The objective of the present invention is to develop a method for the hydrogenation processing of mixtures of inedible plant and petroleum feedstock to obtain diesel fuel with the required low-temperature characteristics, providing for the expansion of the feedstock base for diesel fuel production by involving low-quality gas oils from secondary processes.

To solve this problem, a method is proposed for the joint hydrogenation processing of plant and petroleum feedstock, which differs in that the hydrogenation processing process is carried out in three stages: at the first stage, petroleum feedstock containing up to 40% of low-quality gas oils of secondary origin is hydrotreated on a CoMo catalyst applied to obtain hydrogenate with sulfur content in the range of 150-500 ppm. In the second stage, the hydrogenated product of the first stage is mixed with a lipid fraction extracted from microalgae or with non-food vegetable oil in an amount of not more than 20%, the resulting mixture is subjected to a hydrodeoxygenation process on a catalyst package consisting of massive MoS ₂ and a supported trimetallic NiCoMo catalyst. In the third stage, the resulting product of the second stage is subjected to a hydrodewaxing process on a zeolite-containing NiMo catalyst to achieve the required low-temperature characteristics.

The first stage of hydroprocessing is carried out at a pressure of 4-7 MPa, a temperature of 330-380 ° C, a volumetric feed rate of 1.5-3.0 h ^-1 , a hydrogen-containing gas / raw material ratio of 600-1000 n / v.

The second stage of hydroprocessing is carried out at a pressure of 4-7 MPa, a temperature of 320-380 ° C, a volumetric feed rate of 0.5-1.5 h ^-1 , a hydrogen-containing gas / raw material ratio of 800-1200 n / v.

The third stage of hydroprocessing is carried out at a pressure of 4-5 MPa, a temperature of 270-380 ° C, a volumetric feed rate of 2-3 h ^-1 , a hydrogen-containing gas / raw material ratio of 800-1000 n / v.

The advantage of the method is the possibility of involving sulfur and high-sulfur secondary gas oils in the composition of raw materials and simultaneous exclusion of valuable edible oils and fats from the composition of the raw materials - they are replaced by inedible oils and lipids obtained from algae. Carrying out hydrotreating at the first stage to a residual sulfur content in the range of 150-500 ppm allows, on the one hand, to conduct the process under milder conditions, on the other hand, there is no need to additionally introduce a sulfurizing agent in the second stage to maintain the catalysts in active form. In addition, the use of MoS ₂ as the first catalyst layer in the second stage allows the process of hydrodeoxygenation to be carried out mainly along the route of direct hydrogenation without the formation of carbon oxides that inhibit the hydrodesulfurization reaction [D. Kubicka, L. Kaluza // Appl. Catal. A: Gen. 2010. V. 372. P. 199-208].

The technical result of the present invention is a highly efficient technology that allows you to process a mixture of straight-run diesel fractions, low-quality gas oils of secondary origin and plant raw materials for the production of diesel fuels with improved low-temperature properties. The technical result is achieved through a three-stage processing of raw materials using deposited CoMo, bulk MoS ₂ , deposited NiCoMo and zeolite-containing NiMo catalysts.

Below are examples of specific implementation of the method.

Example 1

A mixture of straight-run diesel fraction (60% by weight) and light gas oils of catalytic cracking (20% by weight) and coking (20% by weight) with a sulfur content of 10361 mg / kg) is subjected to hydrogenation processing. Next, the hydrogenated product of the first stage with a sulfur content of 155 mg / kg is mixed with the lipid fraction extracted from microalgae, the ratio of plant material and hydrogenated product is 5: 95% of the mass, respectively. After hydrodeoxygenation, the 2nd stage hydrogenate is subjected to hydrodewaxing.

The first stage of hydrogenation processing - hydrodesulfurization, is carried out at a pressure of 5 MPa, a temperature of 360 ° C, a volumetric feed rate of 1.5 h ^-1 , a hydrogen-containing gas (HSG) / raw material ratio of 700 n.w./vol., In the presence of aluminum-cobalt-molybdenum hydrotreating catalyst. The resulting hydrogenated product is sent to the second stage of the process - catalytic hydrodeoxygenation and hydrotreating.

The second stage of the process - catalytic hydrodeoxygenation and hydrotreating is carried out at a pressure of 5 MPa, a temperature of 350 ° C, a volumetric feed rate of 1.5 h ^-1 , a ratio of HSG / raw material of 1000 N / v / v, in the presence of a catalytic system consisting of a package of catalysts: massive molybdenum disulfide in the first layer and a nickel-cobalt-molybdenum catalyst based on alumina in the second layer. The resulting hydrogenated product is sent to the third stage of the process - catalytic hydrodewaxing.

The third stage of the process, catalytic hydrodewaxing, is carried out at a pressure of 4 MPa, a temperature of 270 ° C, a space velocity of the feedstock of 3.0 h ^-1 , a ratio of HSG / feedstock of 800 n / v / v, in the presence of a nickel-molybdenum catalyst on a zeolite-containing carrier.

The resulting product is subjected to stabilization and the 180 ° C - CC fraction is withdrawn as a component of diesel fuel with a cloud point of minus 35.3 ° C and a sulfur content of 9 mg / kg.

Example 2

A mixture of straight-run diesel fraction (80 wt%) and light catalytic cracked gas oil (20 wt%) with a sulfur content of 7895 mg / kg) is subjected to hydrogenation processing. Further, the hydrogenated product of the first stage with a sulfur content of 276 mg / kg is mixed with technical rapeseed oil, the ratio of plant raw materials and hydrogenated product is 15: 85% of the mass, respectively. After hydrodeoxygenation, the 2nd stage hydrogenate is subjected to hydrodewaxing.

The first stage of hydrogenation processing - hydrodesulfurization, is carried out at a pressure of 4.5 MPa, a temperature of 340 ° C, a space velocity of the feedstock of 2.5 h ^-1 , the ratio of hydrogen-containing gas (HSG) / raw material - 600 n.w./vol., In the presence of an aluminum-cobalt-molybdenum hydrotreating catalyst. The resulting hydrogenated product is sent to the second stage of the process - catalytic hydrodeoxygenation and hydrotreating.

The second stage of the process - catalytic hydrodeoxygenation and hydrotreating is carried out at a pressure of 4.5 MPa, a temperature of 340 ° C, a space velocity of the feedstock of 0.5 h ^-1 , the ratio of HSG / feedstock - 900 n.w./vol., In the presence a catalytic system consisting of a package of catalysts: massive molybdenum disulfide in the first layer and a nickel-cobalt-molybdenum catalyst based on aluminosilicate in the second layer. The resulting hydrogenated product is sent to the third stage of the process - catalytic hydrodewaxing.

The third stage of the process, catalytic hydrodewaxing, is carried out at a pressure of 4 MPa, a temperature of 290 ° C, a space velocity of the feedstock of 2.0 h ^-1 , a ratio of HSG / feedstock of 800 n.w./about., In the presence of a nickel-molybdenum catalyst on a zeolite-containing carrier.

The resulting product is subjected to stabilization and the 180 ° C - CC fraction is removed as a component of diesel fuel with a cloud point of minus 36 ° C and a sulfur content of 8 mg / kg.

Example 3

A mixture of straight-run diesel fraction (80% by weight) and light gas oil of delayed coking (20% by weight) with a sulfur content of 10635 mg / kg) is subjected to hydrogenation processing. Next, the hydrogenated product of the first stage with a sulfur content of 160 mg / kg is mixed with the lipid fraction extracted from microalgae, the ratio of plant material and hydrogenated product is 10: 90% by weight, respectively. After hydrodeoxygenation, the 2nd stage hydrogenate is subjected to hydrodewaxing.

The first stage of hydrogenation processing - hydrodesulfurization, is carried out at a pressure of 4.5 MPa, a temperature of 350 ° C, a volumetric feed rate of 2 h ^-1 , a hydrogen-containing gas (HSG) / raw material ratio of 600 n.w./vol., In the presence of aluminum-cobalt-molybdenum hydrotreating catalyst. The resulting hydrogenated product is sent to the second stage of the process - catalytic hydrodeoxygenation and hydrotreating.

The second stage of the process, catalytic hydrodeoxygenation and hydrotreating, is carried out at a pressure of 4.5 MPa, a temperature of 330 ° C, a space velocity of the feedstock of 1.0 h ^-1 , a ratio of HSGU raw material of 800 n / v, in the presence of a catalytic system consisting of a package of catalysts: massive molybdenum disulfide in the first layer and a nickel-cobalt-molybdenum catalyst based on alumina in the second layer. The resulting hydrogenated product is sent to the third stage of the process - catalytic hydrodewaxing.

The third stage of the process, catalytic hydrodewaxing, is carried out at a pressure of 4.5 MPa, a temperature of 280 ° C, a volumetric feed rate of 2.0 h ^-1 , a ratio of HSG / raw material of 800 n / v / v, in the presence of a nickel-molybdenum catalyst on a zeolite-containing carrier.

The resulting product is subjected to stabilization and the 180 ° C - CC fraction is withdrawn as a component of diesel fuel with a cloud point of minus 35.5 ° C and a sulfur content of 8 mg / kg.

Example 4

A mixture of straight-run diesel fraction (80 wt%) and light catalytic cracked gas oil (40 wt%) with a sulfur content of 7621 mg / kg is subjected to hydrogenation processing. Next, the hydrogenated product of the first stage with a sulfur content of 351 mg / kg is mixed with non-edible unrefined palm oil, the ratio of plant raw materials and hydrogenated products is 20: 80% of the mass. respectively. After hydrodeoxygenation, the 2nd stage hydrogenate is subjected to hydrodewaxing.

The first stage of hydrogenation processing - hydrodesulfurization, is carried out at a pressure of 5 MPa, a temperature of 340 ° C, a volumetric feed rate of 2.0 h- ¹ , a hydrogen-containing gas (HSG) / raw material ratio of 700 n.w./vol., In the presence of aluminum-cobalt-molybdenum hydrotreating catalyst. The resulting hydrogenated product is sent to the second stage of the process - catalytic hydrodeoxygenation and hydrotreating.

The second stage of the process, catalytic hydrodeoxygenation and hydrotreating, is carried out at a pressure of 5 MPa, a temperature of 350 ° C, a space velocity of the feedstock of 0.5 h ^-1 , a ratio of HSG / feedstock of 800 n / v / v, in the presence of a catalytic system consisting of a package of catalysts: massive molybdenum disulfide in the first layer and a nickel-cobalt-molybdenum catalyst based on aluminosilicate in the second layer. The resulting hydrogenated product is sent to the third stage of the process - catalytic hydrodewaxing.

The third stage of the process, catalytic hydrodewaxing, is carried out at a pressure of 5 MPa, a temperature of 270 ° C, a space velocity of the feedstock of 2.5 h ^-1 , a ratio of HSG / feedstock of 800 n / v / v, in the presence of a nickel-molybdenum catalyst on a zeolite-containing carrier.

The resulting product is subjected to stabilization and the 180 ° C - CC fraction is withdrawn as a component of diesel fuel with a cloud point of minus 37.8 ° C and a sulfur content of 7 mg / kg.

Example 5

A mixture of straight-run diesel fraction (80% by weight) and light gas oil of delayed coking (40% by weight) with a sulfur content of 13101 mg / kg) is subjected to hydrogenation processing. Further, the hydrogenated product of the first stage with a sulfur content of 197 mg / kg is mixed with the lipid fraction extracted from microalgae, the ratio of plant raw materials and hydrogenated product is 20: 80% of the mass, respectively. After hydrodeoxygenation, the 2nd stage hydrogenate is subjected to hydrodewaxing.

The first stage of hydrogenation processing - hydrodesulfurization, is carried out at a pressure of 5 MPa, a temperature of 360 ° C, a volumetric feed rate of 1.5 h ^-1 , a hydrogen-containing gas (HSG) / raw material ratio of 700 n.w./vol., In the presence of aluminum-cobalt-molybdenum hydrotreating catalyst. The resulting hydrogenated product is sent to the second stage of the process - catalytic hydrodeoxygenation and hydrotreating.

The second stage of the process, catalytic hydrodeoxygenation and hydrotreating, is carried out at a pressure of 5 MPa, a temperature of 340 ° C, a space velocity of the feedstock of 1.0 h ^-1 , a ratio of HSG / feedstock of 1200 n / v / v, in the presence of a catalytic system consisting of a package of catalysts: massive molybdenum disulfide in the first layer and a nickel-cobalt-molybdenum catalyst based on alumina in the second layer. The resulting hydrogenated product is sent to the third stage of the process - catalytic hydrodewaxing.

The third stage of the process, catalytic hydrodewaxing, is carried out at a pressure of 4 MPa, a temperature of 270 ° C, a space velocity of the feedstock of 2.0 h ^-1 , a ratio of HSG / feedstock of 800 n.w./about., In the presence of a nickel-molybdenum catalyst on a zeolite-containing carrier.

The resulting product is subjected to stabilization and the 180 ° C - CC fraction is withdrawn as a component of diesel fuel with a cloud point of minus 37.6 ° C and a sulfur content of 8 mg / kg.

Example 6

A mixture of straight-run diesel fraction (80 wt%) and light gas oils of catalytic cracking (10 wt%) and coking (10 wt%) with a sulfur content of 9265 mg / kg) is subjected to hydrogenation processing. Next, the hydrogenated product of the first stage with a sulfur content of 232 mg / kg is mixed with non-edible unrefined soybean oil, the ratio of plant raw materials and hydrogenated product is 15: 85% of the mass, respectively. After hydrodeoxygenation, the 2nd stage hydrogenate is subjected to hydrodewaxing.

The first stage of hydrogenation processing - hydrodesulfurization, is carried out at a pressure of 6 MPa, a temperature of 360 ° C, a volumetric feed rate of 2.3 h ^-1 , a hydrogen-containing gas (HSG) / raw material ratio of 800 n.w./vol., In the presence of aluminum-cobalt-molybdenum hydrotreating catalyst. The resulting hydrogenated product is sent to the second stage of the process - catalytic hydrodeoxygenation and hydrotreating.

The second stage of the process - catalytic hydrodeoxygenation and hydrotreating is carried out at a pressure of 6 MPa, a temperature of 360 ° C, a volumetric feed rate of 1.2 h ^-1 , a ratio of HSG / raw material - 1100 N / v, in the presence of a catalytic system consisting of a package of catalysts: massive molybdenum disulfide in the first layer and a nickel-cobalt-molybdenum catalyst based on aluminosilicate in the second layer. The resulting hydrogenated product is sent to the third stage of the process - catalytic hydrodewaxing.

The third stage of the process - catalytic hydrodewaxing is carried out at a pressure of 4 MPa, a temperature of 290 ° C, a space velocity of the feedstock of 2.5 h ^-1 , a ratio of HSG / feedstock of 800 n.w./vol., In the presence of a nickel-molybdenum catalyst on a zeolite-containing carrier.

The resulting product is subjected to stabilization and the 180 ° C - CC fraction is withdrawn as a component of diesel fuel with a cloud point of minus 36.7 ° C and a sulfur content of 6 mg / kg.

Example 7

A mixture of straight-run diesel fraction (70 wt%) and light gas oils of catalytic cracking (15 wt%) and coking (15 wt%) with a sulfur content of 9813 mg / kg) is subjected to hydrogenation processing. Next, the hydrogenate of the first stage with a sulfur content of 412 mg / kg is mixed with mixed with the lipid fraction extracted from microalgae, the ratio of plant raw materials and hydrogenated product is 10: 90% of the mass, respectively. After hydrodeoxygenation, the 2nd stage hydrogenate is subjected to hydrodewaxing.

The first stage of hydrogenation processing - hydrodesulfurization, is carried out at a pressure of 5 MPa, a temperature of 330 ° C, a volumetric feed rate of 3.0 h ^-1 , a hydrogen-containing gas (HSG) / raw material ratio of 700 N / v, in the presence of aluminum-cobalt-molybdenum hydrotreating catalyst. The resulting hydrogenated product is sent to the second stage of the process - catalytic hydrodeoxygenation and hydrotreating.

The second stage of the process - catalytic hydrodeoxygenation and hydrotreating is carried out at a pressure of 5 MPa, a temperature of 360 ° C, a space velocity of the feedstock of 1.1 h ^-1 , a ratio of HSG / feedstock of 1000 Nv / v, in the presence of a catalytic system consisting of a package of catalysts: massive molybdenum disulfide in the first layer and a nickel-cobalt-molybdenum catalyst based on alumina in the second layer. The resulting hydrogenated product is sent to the third stage of the process - catalytic hydrodewaxing.

The third stage of the process, catalytic hydrodewaxing, is carried out at a pressure of 4 MPa, a temperature of 270 ° C, a space velocity of the feed of 2 h ^-1 , a ratio of HSG / feed of 800 n / v / v, in the presence of a nickel-molybdenum catalyst on a zeolite-containing carrier.

The resulting product is subjected to stabilization and the 180 ° C - CC fraction is removed as a component of diesel fuel with a cloud point of minus 37.3 ° C and a sulfur content of 8 mg / kg.

Claims (4)

1. A method of hydrogenation processing of vegetable and oil raw materials, characterized in that a lipid fraction extracted from microalgae or non-edible vegetable oils is used as a vegetable component, and a straight-run diesel fraction is used as an oil component in a mixture with light gas oils of catalytic cracking and coking; the process of joint hydroprocessing is carried out in three stages: at the first stage, the raw material consisting of straight-run diesel fraction and a mixture of light gas oils of catalytic cracking and coking in a ratio of 60.0-80.0: 20.0-40.0 wt.%, respectively, is subjected to hydrotreating in the presence of a cobalt-molybdenum catalyst based on alumina or aluminosilicate to obtain a hydrogenate with a sulfur content in the range of 150-500 ppm; then, at the second stage of hydro-processing, the raw material consisting of the hydrogenated product of the first stage and the plant component in the ratio 80.0-95.0: 5.0-20.0 wt.%, respectively, is subjected to the hydrodeoxygenation process combined with hydrodesulfurization in the presence of a package of catalysts: massive molybdenum disulfide in the first layer and a nickel-cobalt-molybdenum catalyst based on alumina or aluminosilicate in the second layer; in the third stage of the process, catalytic hydrodewaxing is carried out in the presence of a zeolite-containing nickel-molybdenum catalyst; the resulting product is subjected to stabilization and the 180-kk ° C fraction is withdrawn as a component of diesel fuel. 2. The method according to claim 1, characterized in that the first stage of hydro-processing is carried out at a pressure of 4-7 MPa, a temperature of 330-380 ° C, a volumetric feed rate of 1.5-3.0 h ^-1 , a hydrogen-containing gas / raw material ratio - 600-1000 n / v 3. The method according to claim 1, characterized in that the second stage of hydroprocessing is carried out at a pressure of 4-7 MPa, a temperature of 320-380 ° C, a volumetric feed rate of 0.5-1.5 h ^-1 , a hydrogen-containing gas / raw material ratio - 800-1200 n / a / rev 4. The method according to claim 1, characterized in that the third stage of hydroprocessing is carried out at a pressure of 4-5 MPa, a temperature of 270-380 ° C, a volumetric feed rate of 2.0-3.0 h ^-1 , a hydrogen-containing gas / raw material ratio - 800-1000 n / a / rev