Plant for processing heavy oil residues and method of obtaining distillates of fuel purpose based thereon

FIELD: oil and gas industry.

SUBSTANCE: plant for processing heavy oil residues consists of the raw material heating oven connected with the reactor used for the cracking process, separators and rectification column. The plant is differed by the fact that it is equipped with the acoustical action unit installed in front of the oven and made with the possibility of processing oil residues mixed with liquid aromatic addition, hydraulic cyclone installed after the reactor and made with the possibility of separating hydrogenisate into two fractions: fraction with the boiling temperature of up to 400°C and fraction with the boiling temperature of more than 400°C; at that, hydraulic cyclone is connected through the oven to the hydraulic cleaning reactor of fraction with the boiling temperature of up to 400°C, which is connected to separators and rectification column. Method of obtaining distillates of fuel purpose on the above plant involves mixing of oil stock with hydrogen donator - liquid aromatic addition, homogenisation and activation of the obtained mixture by means of acoustical action under pressure of 0.5-1.0 MPa, temperature of 60-120°C, oscillation frequency of 0.5-50 kHz, intensity of not less than 0.2 W/cm2 and the installed capacity of not less than 5 KW, and performing the thermal hydrogen cracking process of the obtained mixture with the subsequent extraction of end products.

EFFECT: simplifying the design and increasing efficiency.

9 cl, 1 tbl, 1 dwg

 

The technical field

The invention relates to the refining industry, in particular to methods and devices for processing heavy oil residues with obtaining distillate fuel use liquid flavored supplements - effective hydrogen donors.

The level of technology

Currently, oil companies around the world are faced with falling demand for oil, and therefore encourage oil companies to develop new ways of processing that could significantly improve the processing of oil in the light fraction.

Some oil companies believe that to overcome these problems by processing oil fractions with the use of new technologies and equipment operating refineries with the lowest capital costs.

One of the most promising modern ways of solving this problem is joint cracking under hydrogen pressure residual mixture of crude oil, oil shale, and liquid aromatic additive, which is taken in the amount of 1-10% by weight of oil residue (RF patents №2128207, 1999, No. 2261265, 2001).

In the known methods this mixture is subjected to thermal hydrocracking of obtaining fuel distillates.

Closest to us is oedema invention is the installation of heavy oil thermal cracking units and the method for distillate fuel fractions destination and VAT residue of heavy oil (see EN 2058369, publ. 20.04.1996,).

In the known method thermocracking under pressure of 5 MPa is subjected to heavy oil on the installation comprising a mixer heavy oil with organic additive, furnace heating raw materials, thermal reactors, separators, distillation column. Known device provides an output of light distillates at the level of 40-50%.

Known technical solution has the following disadvantages. Used as an additive donor hydrogen shale contains 40-60 wt.%. the mineral, which has a fairly strong erosive properties. In the long run all of the reaction apparatus and especially the throttle valves are subjected to erosion and premature failure. If such equipment is gradual deposition on the walls of the apparatus of the mineral part of oil shale and products of coke formation, which ultimately leads to coking.

In known apparatus design installation of heavy oil thermal cracking units at the stage of preparation of raw materials used mixer, which does not provide uniform distribution of the crushed oil shale in the whole volume of raw materials. Furthermore, this setup allows you to get only the intermediate distillate fractions (raw materials), which contain significant kolichestvennyh compounds (phenols), nitrogenous bases, sulfur and unsaturated compounds.

Such raw materials are necessary in a separate block to be subjected to 2-step Hydrotreating to produce gasoline, kerosene and diesel fuel. In this regard, technology and instrumentation in General, the installation of thermal cracking units of heavy oil under pressure of 5 MPa become unprofitable.

Disclosure of inventions

The present invention is to increase the efficiency of the facility under hydrogen pressure of heavy oil residues and improve the quality of the fuel and distillates, as well as increased erosion resistance of the reaction apparatus and throttle valves, as well as preventing coking of the walls of the installation.

This technical result is achieved by the fact that the installation for the processing of heavy petroleum residues, containing furnace heating raw materials, the reactor for the cracking process, separators and distillation column, according to the invention the installation is equipped with a block of acoustic impact made with the possibility of crude oil residues in the mix with flavored liquid additive, the cyclone made with the possibility of separation of the hydrogenated feed is separated into two fractions: a fraction with a boiling point of about 400°C and the fraction with a boiling point above 400°C, hydrotreater unit fraction of the boiling point of 400°C.

The hydrotreater unit fractions can be filled with a heterogeneous bifunctional catalyst.

As a heterogeneous bifunctional catalysts used allocability, aluminumalloy wolfsangelahnliches and alumopolyethylene.

In addition, the hydrotreater unit fractions made with the possibility of functioning under the pressure of 6-8 MPa at a temperature of 360-380°C.

New installation process activation in the form of acoustic unit exposure it is possible to achieve effective homogenization and activation of raw materials and to get to this stage up to 10-15% light distillates fuel purposes.

The performance of the hydrocyclone with the possibility of separating the hydrogenated feed is separated into two fractions: a fraction with a boiling point of about 400°C and the fraction with a boiling point above 400°C and the rector of the Hydrotreating fraction with BP. up to 400°C increases the efficiency of thermal cracking.

This technical result is also achieved by a method of producing distillate fuel appointment at the facility for processing heavy oil residue comprising a mixture of crude oil with a hydrogen donor, the process of thermal hydrocracking resulting mixture, followed by separation of the desired products. According to the new method as a donor of hydrogen used is t flavored liquid Supplement and the mixture is optionally subjected to homogenization and activation by acoustic impact pressure of 0.5-1.0 MPa, a temperature of 60-120°C, the oscillation frequency of 0.5-50 kHz, an intensity of not less than 0.2 W/cm2and installed capacity of not less than 5 kW.

Thermal hydrocracking expedient for carrying out in continuous mode under hydrogen pressure of 6.0 to 12.0 MPa, the temperature in the reactor 390-435°C and space velocity of the raw materials 1,0-2,5 h-1.

Homogenization and activation of a mixture of acoustic impact allows you to achieve results and to get to this stage up to 10-15% of light fuel distillates.

In such conditions result in destruction of large molecules raw materials (e.g. oil) with the formation of 10-15 wt.%. low molecular weight products (gasoline and diesel fractions).

Acoustic impact of raw material is exposed to significant speed-UPS and more downs, pulses are generated acceleration, which, in turn, excite in the processing environment cavitation, intensifying the process.

Raw materials in the mix with flavored liquid Supplement subjected to processing in units of acoustic impact, enables its thermal hydrocracking in milder conditions, which in turn increases erosion resistance reaction about what orogovenia and throttle valves and prevents coking of the walls of the installation.

Homogenization and activation of the mixture by the acoustic treatment under a pressure of less than 0.5 or more than 1.0 MPa, a temperature of less than 60 or greater than 120°C., a speed of less than 5 or more than 10 m/s, the oscillation frequency is less than 0.5 or more than 50 kHz, an intensity of less than 0.2 W/cm2and installed capacity of less than 5 kW, is not effective and does not contribute to improving the quality of the fuel distillates, and more erosion-resistant equipment.

As raw materials for this type of installations used oil, tar, heavy crude oil, heavy cycle gas oils, heavy bituminous oils extracted from oil Sands, and coal products origin.

The method according to the present invention carried out using the following liquid flavored additives donor hydrogen:

1) oil shale with their boiling temperature of 250-450°C;

2) hydrotreated fraction with boiling within 360-400°From its own production;

3), comprising a hydrotreated fraction with boiling within 360-400°C and the fraction of shale oil 250-450°C in the ratio of 1:0.6 to 1.5;

4), comprising a hydrotreated fraction with boiling within 360-400°C and molybdenum or Nickel catalysts (0.01 to 0.05 wt.% for raw materials).

Target commodity products obtained from thermal hydrocracking in accordance with what Subramaniam, are:

petrol (FR. NICHOLAS - 180°C) grade-80;

- diesel fuel (FR. 180-360°C) cetane number 48-50;

- hydrotreated fraction 360-400°C - liquid flavor additive - donor hydrogen;

- fraction above 400°C is used as boiler fuel or as a risaykl for full turning it into gasoline and diesel fuel.

List of figures

The drawing shows a diagram of installation of thermal cracking with the implementation of the method for producing fuel distillates in this installation.

The implementation of the invention

Installation scheme for the implementation of the proposed method is shown in the drawing. Preparation of raw materials is carried out as follows. In a heated mixer 1, where the temperature of 80-120°C, or other mixing device serves flavored liquid additive from a reservoir (not shown) and raw materials (oil, tar). First mixing device 1 serves raw, then flavored liquid Supplement. In the mixer 1 is pre-mixing 2-component mixture. After the mixer, the mixture is fed to the installation of the acoustic treatment 2, where the effective homogenization of the mixture and activating it, and then raw pump 3 is fed into the heat exchangers 4 and 11 and oven with 5 heating raw materials - section 6. From the furnace 5 is partially converted feedstock enters neither is the Nuits part of the hollow unheated reactor 7 thermal hydrocracking, where under hydrogen pressure 6-12 MPa, the temperature along the height of the reactor 390-435°C and space velocity of the raw materials 1,0-2,5 h-1happen reactions of hydrocracking feedstock. The supply of hydrogen-containing gas is 1000-1200 nm31 m3of raw materials. After the reactor 7, the gas-vapor stream is directed into the cyclone 8, where the temperature of 260-300°C and a pressure of 6 to 11 MPa.

Under these conditions, the top of the hydrocyclone go mostly faction, wikipaedia 360-400°C, bottom - vicipaedia above 400°C. the Upper stream of the hydrocyclone with a hydrogen-containing gas (hydrogen-rich), passing the heating system in section 9 of the furnace 5, is sent to the hydrotreatment reactor 10 filled with a bifunctional heterogeneous catalyst, where under the pressure of 6-8 MPa, a temperature of 360-380°C reactions proceed removal from raw materials heteroatomic and unsaturated compounds. The product after Hydrotreating reactor through the heat exchangers 11 and 4 and the refrigerator 12, comes first in the separator 13 high pressure, which separates everything, then into the separator 14 to the low pressure. Everything from the separator 13 is directed to the circulation compressor 17, after which it is mixed with fresh hydrogen is returned to the process, and part of everything from the separator 13 in the form of Obvodnogo gas is sent for recycling. After the separator 14 low pressure hydrotreated hydrogenation product is sent to rectificate is nnow a clear separation column 15 to obtain commercial products - gasoline, diesel oil and hydrotreated fraction 360-400°C, used as a flavored liquid Supplement. The product from the bottom of the hydrocyclone 8 passes through the throttle valve in the refrigerator 16 and is sent in the form of risaykl or residual fuel oil fraction in the tank farm.

The material balance of thermal hydrocracking of heavy oil residue

Table
Name of raw materials, productswt.%.t/ht/year
I Thermal hydrocracking
I Taken:
- Heavy oil residue100,012,699792,0
Liquid activator (hydrotreated fraction 360-400°C)6,00,766019,2
- Hydrogen1,90,241900,8
Total:107,913,60107712,0
II Received:
1. Hydrocarbon gas C1-C45,10,645068,80
2. The upper stream of the hydrocyclone, including:55,56,9955360,80
- gasoline fraction (NC-180°C)10,01,259900,0
- diesel fraction (180-360°C)a 38.54,8438332,8
- faction 360-400°C - liquid activator7,00,907128,0
3. The bottom stream of the hydrocyclone, including:46,1of 5.8146015,20
the fraction of NK - 360°C5,10,65 5148,0
- faction 360-400°C3,30,413247,2
fraction >400°C37,74,7537620,0
4. Loss1,20,161267,20
Total:107,913,60107712,0
II Hydrotreating fraction of NC - 400°C
III Taken:
- Fraction of NC - 400°C55,56,9955360,80
- Hydrogen1,00,12950,40
Total:56,57,1156311,20
IV Received:0,80,10792,0
- Gas55,77,0155519,2
The hydrogenation product, including:11,01,3810929,6
petrol (MK-180°C)38,24,8038016,0
- diesel fuel (180-360°C)
- faction 360-400°C - liquid activator6,00,755940,0
loss0,50,08633,6
Total:56,57,1156311,20

Technological parameters of operation of the basic apparatus of thermal hydrocracking.

1. The installation process activation

Acoustic impact exercise with the following parameters:

- pressure of 0.5-1.0 MPa;

the temperature of 60-120°C;

frequency fluctuations of 0.5-50 kHz;

- the intensity of not less than 0.2 W/cm2;

the installed capacity is not what the Eney 5 kW.

2. Oven heating raw materials

Section 6

- pressure 6-12 MPa;

the inlet temperature of 60-120°C;

the outlet temperature 460-480°C;

- flue gas temperature of 500-600°C.

Section 9

the inlet temperature of 280-300°C;

the outlet temperature of 360-380°C;

- flue gas temperature of 500-600°C.

3. The reactor thermal hydrocracking

- pressure 6-12 MPa;

the temperature along the height of the reactor 390-435°C;

- volumetric feed rate of 1.0-2.5 hours-1;

- supply all 1000-1200 nm3/m3of raw materials.

4. Hydrocyclone

- pressure 6-11 MPa;

- temperature of 260-300°C.

5. The hydrotreater unit

the pressure of 6-8 MPa;

the temperature along the height of the reactor 360-380°C;

- volumetric feed rate of 1.0-1.2 h-1;

- supply all 600-800 nm3/m3of raw materials.

In the table as example material balance thermal hydrocracking of heavy oil residues, including the stage of thermal hydrocracking feedstock and Hydrotreating fraction of NC-400°C.

According to thermal hydrocracking and method for producing fuel distillates yield of light commodity fuels is 60-65% (based on raw materials.

1. Installation for processing of heavy petroleum residues, containing furnace heating raw material, connected to the reactor for the cracking process, separators and distillation column, Otley is audacia fact, it is fitted with established before the microwave unit of the acoustic treatment made with the possibility of processing oil residue in a mixture of liquid aromatic additive, selected after reactor cyclone made with the possibility of separation of the hydrogenated feed is separated into two fractions: a fraction with a boiling point of about 400°C and the fraction with a boiling point above 400°C, and the hydrocyclone is connected through the furnace with the hydrotreater unit fractions with a boiling point of about 400°C, which is connected to the separators and distillation column.

2. Installation according to claim 1, wherein the Hydrotreating reactor filled with a heterogeneous bifunctional catalyst.

3. Installation according to claim 1, characterized in that the hydrotreater unit has a capability of functioning under the pressure of 6-8 MPa at a temperature of 360-380°C.

4. A method of obtaining a distillate fuel destination on the installation according to claim 1, comprising mixing the crude oil with hydrogen donor is a liquid aromatic additive, homogenization and activating the resulting mixture by acoustic forcing, under pressure of 0.5-1.0 MPa, a temperature of 60-120°C, the oscillation frequency of 0.5-50 kHz, an intensity of not less than 0.2 W/cm2and installed capacity of not less than 5 kW, the process of thermal hydrocracking, the obtained mixture, followed by separation of the target is s products.

5. A method of obtaining a distillate according to claim 4, characterized in that thermal hydrocracking is carried out in continuous mode under hydrogen pressure of 6.0 to 12.0 MPa, the temperature in the reactor 390-435° C and space velocity of the raw materials 1,0-2,5 h-1.

6. A method of obtaining a distillate according to claim 4, characterized in that as the liquid aromatic additives used in shale oil and their boiling temperature of 250-450°C.

7. A method of obtaining a distillate according to claim 4, characterized in that as the liquid aromatic additive use hydrotreated fraction with boiling within 360-400°C.

8. A method of obtaining a distillate according to claim 4, characterized in that as the liquid aromatic additive use, comprising a hydrotreated fraction with boiling within 360-400°C and the fraction of shale oil with their boiling temperature of 250-450°C in the ratio of 1:0.6 to 1.5.

9. A method of obtaining a distillate according to claim 4, characterized in that as the liquid aromatic additive use, comprising a hydrotreated fraction with boiling within 360-400°C and molybdenum and/or Nickel catalysts in the ratio of 1:0.01 to 0.05.



 

Same patents:

FIELD: mining.

SUBSTANCE: invention refers to method of thermal cracking of heavy oil products consisting in their supply together with active donor-hydrogen additive as source raw material into zone of cracking and its heat treatment; as donor-hydrogen additive water is used at amount of 10-50 wt %; source raw material is supplied into zone of cracking in form of water-oil emulsion under overcritical pressure 22.5-35.0 MPa, at which heat treatment is performed at the temperature of 320-480°C.

EFFECT: creating high technological method of thermal cracking of heavy oil residues with increased depth of raw material processing and with increased output of light distillate fractions.

1 ex, 1 tbl

FIELD: petroleum processing.

SUBSTANCE: invention relates to technologies of obtaining feedstock sources such as crude oil, high-boiling petroleum fractions, petroleum residues, coal liquefaction and by-product-cock plant products, spent lubricating oils, household and industrial wastes of various hydrocarbon fuels, and hydrocarbon raw materials for basic and petrochemical synthesis. Method according to invention comprises: provision and/or synthesis hydrogen donors; hydrocarbon, hydrogen donor, and catalyst stirring step; separation of resulting mixture; isolation of light and heavy fractions; and recycling of heavy fraction together with catalyst to mixing step and hydrogenation of light fraction followed by recovering synthesized hydrogen donors, which are also directed to mixing step.

EFFECT: enhanced process efficiency.

9 cl, 1 dwg, 4 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: to crude oil with 2-10% water content is added catalyst followed by activation of hydrogen donors and hydrogenation of crude oil. Catalyst is used in the form of water-soluble group VI and VIII element compounds, which dissolves in water contained in crude oil to form true solution. Hydrogen donors are own crude oil fractions and products obtained from own crude oil fractions.

EFFECT: simplified and deepened oil processing.

10 cl, 1 dwg, 1 tbl

The invention relates to a catalyst and method of improving the grade of heavy hydrocarbons, which provides a high degree of conversion of heavy hydrocarbons into lighter, more valuable hydrocarbon products

FIELD: chemistry.

SUBSTANCE: invention refers to the device for transformation of hydrocarbon row material and water mixture representing the body whereat the chamber is formed with to opposite walls designed as a fragment of second-degree surface inversely positioned relative to each other; in the other walls the holes are made for forming of the channels feeding under the pressure the hydrocarbon row material and water. The longitudinal axis of the channel holes are displaced relative to each other in order to direct the flow of hydrocarbon row material flow to one wall and the water flow - to another with both flows being in the form of second-degree surface fragment. The body is provided with cylindrical channel connected with chamber, it longitudinal axis is perpendicular to the longitudinal axes of the channels feeding under the pressure the hydrocarbon row material and water; in the recess of the cylindrical channel along its longitudinal axis one discharger electrode is located, its second electrode is fixed on the inner wall of this channel with electrodes switching to energy supply which design provides the possibility of voltage and/or current control. Invention also refers to the method for transformation of water/hydrocarbon row material mixture by the action of electricity implemented in the claimed device.

EFFECT: improvement of the method.

2 cl, 2 tbl, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention refers to the bifunctional catalyst possessing the hydrogenising as well as acid function. The method for the preparation of the catalyst for hydrocarbon conversion includes: (a) obtaining of complex compounds as precursors of non-crystalline inorganic oxide with mesopores disorderedly connected together; (b) usage of the complex compounds from stage (a) for the preparation of the composite containing zeolite incorporated into inorganic oxide with mesopores disorderedly connected together; (c) incorporation of the at least one metal possessing the hydrogenising function to the composite obtained on the stage (b).

EFFECT: obtaining of the catalyst with enhanced operational versatility for control of the acid and hydrogenising functions.

13 cl, 13 ex, 3 tbl, 5 dwg

FIELD: mining.

SUBSTANCE: invention refers to method of thermal cracking of heavy oil products consisting in their supply together with active donor-hydrogen additive as source raw material into zone of cracking and its heat treatment; as donor-hydrogen additive water is used at amount of 10-50 wt %; source raw material is supplied into zone of cracking in form of water-oil emulsion under overcritical pressure 22.5-35.0 MPa, at which heat treatment is performed at the temperature of 320-480°C.

EFFECT: creating high technological method of thermal cracking of heavy oil residues with increased depth of raw material processing and with increased output of light distillate fractions.

1 ex, 1 tbl

FIELD: oil and gas industry.

SUBSTANCE: invention refers to method for simultaneous making medium fractions and lubricant bases from synthetic paraffin mixtures, including hydrocracking stage (i) and distillation of product of stage (i), where hydrocracking involves addition of solid bifunctional catalyst including: (A) acidic carrier consisting of catalystically active porous solid substance, including silicon, aluminium, phosphorus and oxygen interlinking so that to form mixed amorphous solid substance, characterised by nuclear ratio Si/Al within 20 to 250, ratio P/Al at least 0.1, but lower that 5, total porous amount within 0.5 to 2.0 ml/g, average pore diameter within 2 nm to 40 nm and specific surface area within 200 to 1000 m2/g; (B) at least one metal with hydrogenation-dehydrogenation activity, selected from groups with 6th on 10th of Periodic systems and distributed over specified carrier (A) in amount within 0.05 to 5 wt % relative to total mass of catalyst.

EFFECT: development of method for simultaneous making medium fractions and lubricant bases from synthetic paraffin mixtures.

25 cl, 26 ex, 5 tbl, 2 dwg

FIELD: technological processes; metallurgy.

SUBSTANCE: heavy hydrocarbon fraction, previously heated up to 60-350°C, is exposed to plasma for hydrocarbon molecules splitting into atoms in high temperature area without oxygen access, further "bombardment" of other hydrocarbon chains with them, their crushing and hydrogenation in reaction zone, which results in creation of light hydrocarbon fractions, at that plasma represents ionised high-temperature gas.

EFFECT: simplification of technology for plasmochemical hydrocracking of heavy hydrocarbon raw material, combination of heavy hydrocarbon fractions cracking and hydrogenation into single process, possibility to adjust extent of hydrocarbon molecules crushing with time of their bombardment with hydrogen and carbon atoms and temperature of raw material supplied into reactor, provision of possibility for device to operate in several technological modes.

3 cl, 1 dwg, 1 tbl

FIELD: chemistry.

SUBSTANCE: stable composition for application for catalyst carrier impregnation in order to obtain catalytically active solid substance includes: (A) water; (B) catalytically active metals, which are in form of and containing: (1) at least, one component, ensuring, at least, one metal of group VIB of Periodic system; and (2) at least, one component, ensuring, at least, one metal of group VIII of Periodic system, selected from group consisting of Fe, Co and Ni; and (i) said metal of group VIII is supplied with, in fact, insoluble in water component; (ii) molar ratio of said metal of group VIII and metal of group VIB constitutes approximately from 0.05 to approximately 0.45, on condition that amount of said metal of group VIII is sufficient for promoting catalytic impact of said metal of group VIB; (iii) concentration of said metal of group VIB, expressed as oxide, constitutes, at least, from approximately 3 to approximately 50 wt % of said composition weight; and (C) at least, one, in fact, water-soluble phosphorus-containing acid component in amount, insufficient for dissolving said metal of group VIII at room temperature, and sufficient for ensuring molar ratio of phosphorus and metal of group VIB from approximately 0.05 to less than approximately 0.25. Described is method of obtaining described above composition, including addition to suitable water amount of: (A) at least, one in fact water-insoluble component based on metal of group VIII, selected from group consisting of Fe, Co and Ni; and (B) at least, one in fact water-soluble phosphorus-containing acid component in amount insufficient for causing dissolution of said component based on metal of group VIII, with obtaining suspension, and combining suspension with: (C) at least, one component based on metal of VIB group; and (D) mixing of combinations (A), (B) and (C), and heating mixture during time and to temperature sufficient for formation of solution by (A), (B) and (C); and (E) adding supplementary amount of water, if necessary, in order to obtaining concentrations of solution of, at least, one said metal of group VIII, at least, one said metal of group VIB and phosphorus, suitable for impregnation of said carriers; group VIB and VIII refer to groups of periodic system of elements. Described is catalyst obtained by carrier impregnation with stable composition, suitable for hydrocarbon raw material processing.

EFFECT: increase of conversion degree of sulphur, microcarbon residue.

23 cl, 3 ex

FIELD: chemistry.

SUBSTANCE: stable composition for application for catalyst carrier impregnation in order to obtain catalytically active solid substance includes: (A) water; (B) catalytically active metals, which are in form of and containing: (1) at least, one component, ensuring, at least, one metal of group VIB of Periodic system; and (2) at least, one component, ensuring, at least, one metal of group VIII of Periodic system, selected from group consisting of Fe, Co and Ni; and (i) said metal of group VIII is supplied with, in fact, insoluble in water component; (ii) molar ratio of said metal of group VIII and metal of group VIB constitutes approximately from 0.05 to approximately 0.45, on condition that amount of said metal of group VIII is sufficient for promoting catalytic impact of said metal of group VIB; (iii) concentration of said metal of group VIB, expressed as oxide, constitutes, at least, from approximately 3 to approximately 50 wt % of said composition weight; and (C) at least, one, in fact, water-soluble phosphorus-containing acid component in amount, insufficient for dissolving said metal of group VIII at room temperature, and sufficient for ensuring molar ratio of phosphorus and metal of group VIB from approximately 0.05 to less than approximately 0.25. Described is method of obtaining described above composition, including addition to suitable water amount of: (A) at least, one in fact water-insoluble component based on metal of group VIII, selected from group consisting of Fe, Co and Ni; and (B) at least, one in fact water-soluble phosphorus-containing acid component in amount insufficient for causing dissolution of said component based on metal of group VIII, with obtaining suspension, and combining suspension with: (C) at least, one component based on metal of VIB group; and (D) mixing of combinations (A), (B) and (C), and heating mixture during time and to temperature sufficient for formation of solution by (A), (B) and (C); and (E) adding supplementary amount of water, if necessary, in order to obtaining concentrations of solution of, at least, one said metal of group VIII, at least, one said metal of group VIB and phosphorus, suitable for impregnation of said carriers; group VIB and VIII refer to groups of periodic system of elements. Described is catalyst obtained by carrier impregnation with stable composition, suitable for hydrocarbon raw material processing.

EFFECT: increase of conversion degree of sulphur, microcarbon residue.

23 cl, 3 ex

FIELD: chemistry.

SUBSTANCE: in method of obtaining distillates and residues for oil bases from hydrocarbon charge: a) charge is subjected to cracking in presence of hydrogen and hydrocracking catalyst, at least, in one reactor with boiling layer with possibility of conversion, at least, of 10 wt % of charge fraction, boiling at temperature over 370°C, into compounds with boiling point lower than 370°C; b) at least, part of effluent, obtained at stage a), is fractioned for isolation of, at least, first residue, at least, 85 wt % of whose compounds start boiling at temperature 320°C, said first residue containing aromatic compounds; c) at least, part of aromatic compounds from, at least, part of first residue is removed in order to obtain effluent with low content of aromatic compounds, content of aromatic compounds being less than 30 wt %; d) at least, part of effluent, obtained at stage c) is fractioned in order to isolate second residue for oil bases with output , at least, 15 wt % with respect to charge.

EFFECT: possibility to combine production of high-quality lubricating oils with performing preliminary cracking in reactor with boiling layer.

10 cl, 5 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: in method of obtaining distillates and residues for oil bases from hydrocarbon charge: a) charge is subjected to cracking in presence of hydrogen and hydrocracking catalyst, at least, in one reactor with boiling layer with possibility of conversion, at least, of 10 wt % of charge fraction, boiling at temperature over 370°C, into compounds with boiling point lower than 370°C; b) at least, part of effluent, obtained at stage a), is fractioned for isolation of, at least, first residue, at least, 85 wt % of whose compounds start boiling at temperature 320°C, said first residue containing aromatic compounds; c) at least, part of aromatic compounds from, at least, part of first residue is removed in order to obtain effluent with low content of aromatic compounds, content of aromatic compounds being less than 30 wt %; d) at least, part of effluent, obtained at stage c) is fractioned in order to isolate second residue for oil bases with output , at least, 15 wt % with respect to charge.

EFFECT: possibility to combine production of high-quality lubricating oils with performing preliminary cracking in reactor with boiling layer.

10 cl, 5 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: in the caustic reactor for hydrocarbons the source of oxygen and the source of hydrocarbons are burnt and the obtained synthetic gas is used for initiation of a gas-phase reaction for ennobling heavy crude oil.

EFFECT: ennobling reaction is quickly extinguished after initiation of the gas-phase reaction.

42 cl, 1 ex, 8 tbl, 11 dwg

FIELD: petroleum processing.

SUBSTANCE: catalyst contains 15-30% hydrogenation components including groups VU and VIII metals, 20-40% acid component, and 1-4% promoter, the rest being binder: alumina, aluminosilicate, clay, or their mixture. Catalyst is distinguished by having three-component system composed by nickel, molybdenum, and tungsten in the form of their oxides at weight ratio Ni/Mo/W equal to 25:35:40. Above-mentioned acid component contains aluminum fluoride and promoter contains boron oxide and/or zirconium oxide. Preparation technology is simple and completely suppresses production of waste water. Invention describes hydrocracking process in presence of the claimed catalyst, which is carried out at 380-430оС, pressure 3 to 10 MPa, and volume flow rate 1 -3 h-1 at H2/feedstock ratio 250 to 1000. Process is especially appropriate for diesel fuel production.

EFFECT: enabled preparation of high-activity and high-selectivity catalyst at any catalyst production plant without additional equipment.

2 cl, 3 tbl, 7 ex

FIELD: petrochemical processes.

SUBSTANCE: petroleum fractions are treated at elevated hydrogen pressure and temperature in presence of catalytic systems composed catalysts endowed with functions of varying hydrocarbon composition and removing heterorganic compounds. Process is carried out on catalytic base consisting of two or more catalyst and temperature at least 300оС, pressure at least 3.0 MPa, and hydrogen-to-feed volume ratio (nm3/m3) calculated by formula: A=B+C+D, where B is hydrogen-to-feed volume ratio for hydrogenolysis of heterorganic compounds (nm3/m3); C the same for hydrogenation of unsaturated compounds; and D the same for conversion of high-boiling hydrocarbons.

EFFECT: increased yield of light fractions with improved environmental characteristics.

9 cl, 8 tbl, 18 ex

FIELD: petrochemical processes.

SUBSTANCE: hydropyrolysis of hydrocarbon feedstock is effected in tubular pyrolysis furnace in presence of steam and hydrogen. Hydrocarbon feedstock is, in particular, a mixture of gasoline and hydrogenated C9+-fraction of liquid pyrolysis products isolated as side-cut distillate from bottom residue obtained in fractionation of C6-C10+-fraction of liquid pyrolysis products to produce benzene-toluene fraction, the two mixture components being taken at weight ratio (70-80):(20-30), respectively. Molar ratios hydrogen/hydrocarbon feed and hydrogen/C9+-fraction are (1-3):1 and (5.3-15.85):1, respectively.

EFFECT: increased yield of benzene-toluene fraction and benzene content in aromatic fraction of liquid pyrolysis products.

1 tbl, 3 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: to crude oil with 2-10% water content is added catalyst followed by activation of hydrogen donors and hydrogenation of crude oil. Catalyst is used in the form of water-soluble group VI and VIII element compounds, which dissolves in water contained in crude oil to form true solution. Hydrogen donors are own crude oil fractions and products obtained from own crude oil fractions.

EFFECT: simplified and deepened oil processing.

10 cl, 1 dwg, 1 tbl

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: to crude oil with 2-10% water content is added catalyst followed by activation of hydrogen donors and hydrogenation of crude oil. Catalyst is used in the form of water-soluble group VI and VIII element compounds, which dissolves in water contained in crude oil to form true solution. Hydrogen donors are own crude oil fractions and products obtained from own crude oil fractions.

EFFECT: simplified and deepened oil processing.

10 cl, 1 dwg, 1 tbl

FIELD: methods of production of hydrogen, electrical power and the hydraulically purified products out of hydrocarbon raw materials.

SUBSTANCE: the invention is pertaining to the method of production of hydrogen, electrical power and, at least, one hydraulically purified product out of the hydrocarbon raw material containing at least a fraction, which has the same range of boiling-out or higher, than the temperature range of boiling of a hydraulically purified product, which will be produced; this method includes the following operations: treatment of the hydrocarbon raw material with hydrogen at presence of the applied catalyst; at that hydrogen at least partially is produced from fraction of the hydraulically purified raw material having the temperature range of boiling different from the temperature range of boiling of the fraction of hydrocarbon raw material, from which will be produced a hydraulically purified product or at least from a part of the indicated product of the hydraulical purification; separation of the hydraulically purified product from the hydraulically purified raw material, when the hydraulically purified product is necessary to separate; a part or the whole rest hydraulically purified raw material and hydraulically purified product, if it will not be separated to produce hydrogen; a part or all hydrogen, which is not used for treatment of hydrocarbons, is subjected to processing with production of electrical power; or a part of the hydraulically purified raw material and the hydraulically purified product, if it will be not separated, is subjected to processing with production of an electrical power; and the rest is directed to processing with production of hydrogen. The invention allows to produce simultaneously hydrogen, electrical power, and at least one hydraulically purified hydrocarbon product.

EFFECT: the invention allows to produce simultaneously hydrogen, electrical power, and at least one hydraulically purified hydrocarbon product.

18 cl, 1 dwg, 9 ex

Up!