RU2785501C1 - Method for production of petroleum needle coke by delayed coking and installation for implementation of such a method - Google Patents

Abstract

FIELD: oil refining.

SUBSTANCE: invention relates to the field of oil refining, in particular to a method and an installation for the production of highly anisotropic petroleum needle coke by delayed coking. The method includes the use of at least three streams of source raw materials, one of which is highly aromatized, and the rest for less flavored raw materials, while all streams of raw materials are derivatives of secondary oil refining, while less aromatized raw materials are sent to heating and thermo-polycondensation, after which they are sent to a distillation column, from a cube of which raw materials are sent to coking with preheating, coking gas oil returns to the distillation column, heavy gas oils are partially sent from the distillation column to a recycle for thermo-polycondensation, and highly aromatized raw materials are sent for mixing to a stream at an outlet of a thermo-polycondensation reactor, at a ratio selected so that a temperature at an inlet to the distillation column does not exceed 350°C. The installation includes at least three supplies of source raw materials, one of which is highly aromatized, lines for supply of less aromatized streams of raw materials are brought to a furnace for heating of thermo-polycondensation raw materials, which is connected to the thermo-polycondensation reactor, at the outlet of which the line for supply of raw materials is sent to the distillation column. Further, from the cube of the distillation column, a process line is sent to coke chambers through a furnace for coking of raw materials, while the coke chamber is connected by a line for return of coking gasoil to the distillation column, a line for output of heavy gasoil from the distillation column is divided into an input to the furnace for heating of thermo-polycondensation raw materials, a line of input into the distillation column, and an output as a product, and highly aromatized source raw materials are sent for mixing to a stream at the outlet of the thermo-polycondensation reactor into the line for supply to the distillation column.

EFFECT: creation of a method and an installation for the production of needle coke with preliminary preparation of raw materials.

13 cl, 1 dwg, 1 tbl, 14 ex

Description

The invention relates to the field of oil refining, in particular, to a method for producing highly anisotropic petroleum needle coke by delayed coking. The invention can be used for the preparation of raw materials and the subsequent production of needle (anisotropic) coke, for the production of graphite products (steel-smelting electrodes, etc.).

Anisotropic (needle) coke has a pronounced orderly directed fiber structure, is characterized by a low content of heteroimpurities (sulfur, nitrogen, metals), high specific density and good graphitization (the ability to take on a crystalline, layered structure of graphite at high temperatures of about 3000°C). Needle coke is a demanded raw material for the production of graphite products operated under harsh conditions of 3000°C or more (electrodes for metallurgy, structural materials, etc.). In the production of needle coke, the main components of raw materials are highly aromatic fractions of secondary oil refining processes. The technological mode requires an increased coking time of 36÷48 hours, an increase in the recirculation ratio and, as a result, a decrease in the productivity of the plant for fresh feedstock.

Traditionally, decantoils are used as feedstock for the production of needle coke - heavy catalytic cracking gas oils freed from catalyst dust from modern FCC plants. Decantoil is characterized by high density, contains a large amount of aromatic hydrocarbons, low coking capacity compared to straight-run residues, and a rather light fractional composition.

Low-boiling fractions contained in decantoil practically do not participate in coke formation, entering the coke chambers, they evaporate and are removed in the vapor phase together with the coking distillate into the distillation column. This reduces the output of coke to the original decantoil, even if coking is carried out with a high recirculation ratio.

In addition, light-boiling fractions, evaporating, can disturb the hydrodynamic situation in the coke chambers, which contributes to the formation of a highly anisotropic structure of needle cokes.

From the prior art there are many solutions aimed at obtaining petroleum coke, in particular needle coke.

An established technological solution is the use of distillation columns to ensure the formation of raw materials for subsequent coking from the heaviest fractions. Along with this, traditionally in the technological process, heating of raw materials is practiced before being fed to coking. In confirmation of this, we can consider the technological scheme known from the prior art [Reference. Processes of oil refining. Supplement to the journal "Oil and Gas Technologies / Oil and Gas Technologies, No. 2 February 2009 / M: Fuel and Energy / 2009 / 108 s], in which the raw material is fed directly into the distillation column, where it is combined with the recirculating coking product, and then sent with preheating for coking. Or a more complex variation of the technology, close to real production conditions, replicated by ABB Lummus Global [Malik Ram, Gary and Hamilton, "Delayed coker design considerations and project execution", NPRA 2002 Annual Meeting, March 17-19, 2002], where raw materials, heated in the heat exchanger enters the bottom of the distillation column, where it mixes with the condensed recirculation product. The mixture is pumped through the furnace, in which it is heated to a predetermined temperature, and sent for coking.

However, the solutions presented involve the formation of coking feedstock from certain fractionation products in a distillation column, while there are options for supplying coking oil products obtained from primary or secondary oil refineries as raw materials, as evidenced by solutions known from the prior art.

It should be noted that the evolution of the technological process for obtaining needle coke includes the processes of weighting the raw materials, referred to as thermal condensation or thermopolycondensation. For the purposes of the present invention, the term thermopolycondensation is used as follows:

Thermal polycondensation of coking feedstock is a process of heat treatment of distillate feedstock aimed at conducting chemical radical chain reactions, the purpose of which is to obtain aromatic compounds with a high molecular weight.

The prior art method for producing petroleum needle coke [RU 2717815, publication: 03/25/2020], including heating decantoil as a feedstock, mixing it in a column for the formation of secondary raw materials equipped with mass transfer devices, with recirculation to form secondary raw materials, heating secondary raw materials to the coking temperature and coking in coke chambers to obtain needle coke and coking distillate, which is fed into the lower part of the distillation column for fractionation to produce hydrocarbon gas, gasoline, light and heavy coking gas oils and bottoms residue, coke steaming with steam and water cooling, supply products of steaming and cooling into an absorber equipped with mass transfer devices for absorption of high-boiling oil products and separation of products of steaming and cooling in the absorber into vapor and liquid phases, while low-boiling hydrocarbons from the upper part of the column for the formation of secondary raw materials are sent to the abs. order.

A known method for producing petroleum coke [RF Patent No. 2209826, IPC C10B 55/00, publ. 10.08.2003]. This invention presents a method for producing petroleum coke by delayed coking, including heating the primary raw material, separating it into light fractions and a heavy residue in an evaporator, fractionating light fractions in a distillation column together with vapor-liquid coking products, mixing a heavy residue from an evaporator with a bottom residue of a distillation column with the formation of secondary raw materials, its subsequent coking with the production of coke and the supply of steam-gas coking products to the bottom of the distillation column. The quality and quantity of heavy coking gas oil and bottoms are controlled by changing the amount of heavy gas oil supplied as reflux to the mass transfer devices at the bottom of the distillation column.

Also known is the method [US 2022089955; publication: 03/24/2022] which produces high quality graphite/needle grade coke with reduced levels of impurities and improved coefficient of thermal expansion using integrated hydrotreating, catalytic cracking and coking sections, using a combination of a highly paraffinic hydrotreated VGO stream and an aromatic CLO stream, which is then recycled. in the delayed coking area. In this solution, two feed streams are mixed, while the heaviest fraction obtained in the intermediate column, the purpose of which is the formation of a homogeneous primary feed mixture, is sent further to the main distillation column, from the cube of which the heavy fractions are sent for heating, and then to the chambers coking. This solution is the closest to the present invention and can be considered as a prototype.

However, the technical solution described in the prototype does not use the additional possibilities of preparing raw materials for coking by thermal polycondensation of raw materials, and is also not optimal from the point of view that the stream from the coke chamber returned to the distillation column (non-coking raw materials and lighter fractions) may contain valuable from the point of view of obtaining the final product, raw materials, which, when fractionated in a distillation column, will be removed from the process, which negatively affects the % yield of the target product - needle coke.

The technical result of the invention is the creation of a method and installation for the production of needle coke with preliminary preparation of raw materials.

The achievement of the result is ensured by solving the problem of production of petroleum needle coke by delayed coking, where at least three streams of feedstock are used, one of which is highly aromatized, and the rest are less aromatized components of the feedstock, while all feedstock streams are derivatives of secondary oil refining products, in which less flavored feed streams are sent for heating and thermal polycondensation at a temperature of 410-500°C for 30-90 minutes, after which a distillation column is sent, from the bottom of which the raw material is sent for coking with preheating, coking gas oil is returned to the distillation column, heavy gas oils from the distillation columns are partially recycled for thermopolycondensation, and highly aromatic raw materials are sent for mixing to the stream at the outlet of the thermopolycondensation reactor in a ratio selected so that the temperature at the inlet to the rectifier cationic column did not exceed 350°С.

To implement this method, an installation is provided in which at least three sources of feedstock are used, one of which is highly aromatized, the supply lines for less aromatized feed streams are connected to the thermal polycondensation raw material heating furnace, which is connected to the thermopolycondensation reactor at the outlet of which the raw material supply line is sent to distillation column, from the cube of the distillation column, the technological line is sent to the coke chambers through the coking feedstock furnace, while the coke chamber is connected by the coking gas oil return line to the distillation column, the heavy gas oils output line from the distillation column is divided into distillation column and output as a product, and the highly aromatic feedstock is sent for mixing to the outlet stream from the thermopolycondensation reactor to the feed line to the distillation column.

In FIG. 1 shows the installation diagram, where:

1 Heat exchange equipment (heater)

2 Raw material thermopolycondensation oven

3 Thermopolycondensation reactor

4 Main distillation column

5 Raw coking furnace

6 Coke chambers (coking reactors)

7 Heat exchange equipment (refrigerator)

8 Heavy gas oil accumulator

9 Light gas oil accumulator

Flows shown in the diagram:

I Primary raw material

II Secondary raw material of coking

III Cox

IV Coking gases

V Gasoline coking (naphtha)

VI Light gas oil

VII Heavy gas oil

Installation for the implementation of the invention is arranged as follows:

The installation provides for at least three feedstock supply lines, one of which is designed for highly aromatic raw materials, and the rest for less flavored raw materials. The flow lines, with the exception of highly flavored raw materials, are combined into one production line through shut-off and control devices (not shown in Fig. 1), then they are brought to the heater (1). The heater (1) is connected to the furnace (2), after which the thermopolycondensation reactor is placed in series. From the thermopolycondensation reactor, the technological line is sent to the main distillation column (4), this is the line for supplying raw materials that have undergone thermal polycondensation for fractionation, to which recirculating flows are supplied. The column (4) includes a heavy gas oil accumulator (8) and a light gas oil accumulator (9). From the top of the column (4) process outputs for gaseous products and light gas oils through the coolers (7) divert these products. The technological line from the cube of the column (4) is sent to the coke chambers (6) through the coking feedstock furnace (5). The upper part of the coke chambers is connected to the lower part of the column (4). The removal of heavy gas oil from the distillation column (4) is partially sent to two recycles - to the inlet to the furnace for heating the thermopolycondensation feedstock and to the feed line of the feedstock that has undergone thermopolycondensation with pre-cooling, the feed line of the initial highly flavored feedstock is also connected there. A refrigerator, a heat exchanger, a throttling device, etc. can be used as a cooling device.

The number and weight and size dimensions of the coking chambers are determined by technological feasibility, the weight and size dimensions of the remaining devices are determined in accordance with the capacity of the plant for processed raw materials and technological calculation.

The coke chamber (6) filled with coke is first steamed with water vapor, then the coke chamber is cooled with water, after which the coke is extracted. During these processes, the feed of secondary raw materials is switched to a parallel coke chamber to ensure a continuous technological process. The number of coke chambers, which should be at least two, in particular versions of the technological installation, their number is determined by the cycles of their operation and coke extraction with associated services, their volume and the volume of secondary raw materials supplied.

The installation will allow to implement the method according to the invention.

Raw material:

A. Highly flavored feedstocks: low sulfur, catalytic cracking (FCC) decantoils, heavy pyrolysis tars, coal tars and pitches;

B. Medium flavored raw materials low sulfur heavy residues of secondary processes extracts of oil production, heavy diesel fractions of catalytic cracking;

C. Low-aromatized raw materials: low-sulphur vacuum and atmospheric residues of oil distillation, slacks and petrolatums from oil production.

A mixture of components of the feedstock (I) V.S. comes to the plant from the tank farm, or directly from the plant's process units. Due to the heat of internal flows, the raw material preheated in the heat exchange equipment (1) is mixed with heavy coking gas oil (VII) and sent to the reaction coil of the thermopolycondensation furnace (2). The raw mixture is heated in a furnace to a temperature of 410÷500°C and then enters the thermopolycondensation reactor (3), which is a vertical displacement apparatus. In the furnace-reactor system, at high temperature, pressure and due to the time factor, chemical reactions of cracking, aromatization and compaction of aromatic hydrocarbons proceed according to the radical chain mechanism.

At the outlet of the reactor, the mixture of thermopolycondensation products is cooled by mixing with the highly aromatic component of the primary raw material (I) A. and cooled circulating heavy coking gas oil. With a temperature of 300-350°C, the raw mixture enters the contact devices of the separation section of the main distillation column (4). Steam-gas coking products with a temperature of 380-430°C are introduced into the feed part of the column.

With the joint fractionation of the incoming feed streams and delayed coking products, high-boiling, liquid hydrocarbons with a temperature of 360-380°C are concentrated in the bottom part of the column and form highly aromatic secondary coking feedstock (II). The specified flow, after heating to a temperature of 450 - 500 ˚C in the coking feedstock furnace (5), is sent to the coke chamber (6).

The coking process proceeds at a temperature of 450-500°C, an overpressure of 0.3-0.5 MPa, for 32-48 hours. The coking time and the technological mode of the process depend on the filling rate of the coke chamber and the requirements for commercial needle coke. In the course of filling the coke chamber, the coking products are constantly withdrawn to the main distillation column for separation and subsequent qualified processing.

At the end of the coking cycle and the filling of the coke chamber, the flow of secondary raw materials is transferred to a pre-prepared and heated coke chamber. The apparatus removed from coking is subject to maintenance, steaming, cooling of the produced coke with water, its hydraulic extraction and shipment to the consumer are carried out. Utilization of hydrocarbons released during the maintenance of the coke chamber is carried out together with the gas-vapor products of the delayed coking process - this is not the subject of the present invention and is not shown in the diagram.

Uncondensed gas-vapor products of coking in the main distillation column are subjected to rectification.

The heavy coking gas oil (VII) is collected in the accumulator (8) and is: 1) part of the recycled thermopolycondensation feedstock, 2) a cooling stream of thermopolycondensation products, 3) a commercial product of the delayed coking unit.

Light coking gas oil (VI) from the accumulator (9) after cooling is removed from the plant as a component of diesel fuels.

From the top of the distillation column, after cooling and separation, gaseous hydrocarbons (IV) are processed separately or are a component of the fuel. The liquid phase of coking gasoline (V) is sent for further processing.

The industrial applicability and feasibility of the invention is also illustrated by a number of examples. The ratio of flows according to the invention, during the experiments, was selected with the following recirculation ratio. Data on the tests (experiments) carried out are grouped in tab. one.

Example 1

Raw material: ratio A / B / C respectively: 60 / 30 / 10. The mixture of feedstock components B and C enters the plant. After mixing with recirculation, thermopolycondensation occurs at the following parameters:

Temperature: 410°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

After that, mixing with highly aromatic raw materials takes place, flow A, after which the total flow is sent to the column, from the bottom of which secondary raw materials are taken for coking. In this case, the recirculation ratio of the gas oil discharged from the column is 2.5 wt.

After preheating to a temperature of at least 450°C, the secondary raw material stream from the bottom of the column is subjected to coking under the following parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The output of coke on the feedstock, wt., (A, B, C): 25%.

Coke quality, score: 5.0.

Example 2

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 480°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 33.8%. Coke quality, score: 5.5.

Example 3

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.2 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 33.4%. Coke quality, score: 5.5

Example 4

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 2.2 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 33.6%. Coke quality, score: 5.5.

Example 5

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 30 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 32.8%. Coke quality, score: 5.5

Example 6

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 90 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 34.2%. Coke quality, score: 5.5.

Example 7

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 1.8, wt. The yield of coke on the feedstock, wt., (A, B, C): 29.2%. Coke quality, score: 5.0

Example 8

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 2.8, wt. The yield of coke on the feedstock, wt., (A, B, C): 34.8%. Coke quality, score: 5.7.

Example 9

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 450°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 32.6%. Coke quality, score: 5.0

Example 10

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 490°C;

Pressure: 0.4 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 32.6%. Coke quality, score: 5.5.

Example 11

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.3 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 32.8%. Coke quality, score: 5.5

Example 12

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.45 MPa;

Time: 2520 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 33.3%. Coke quality, score: 5.5.

Example 13

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2160 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 30.0%. Coke quality, score: 5.4

Example 14

Similar with the only differences that:

Thermopolycondensation parameters:

Temperature: 440°C;

Pressure: 1.4 MPa;

Thermopolycondensation time: 60 min.

Coking parameters:

Temperature: 480°C;

Pressure: 0.4 MPa;

Time: 2880 min.

The recirculation ratio is 2.5, wt. The yield of coke on the feedstock, wt., (A, B, C): 35.1%. Coke quality, score: 5.7.

Table 1. Test parameters

No. General process indicators Thermopolycondensation parameters Coking parameters Yield of coke on feedstock, wt % coke quality,
score Raw materials,% mass Total raw materials, % mass Raw material productivity, % mass Recycle productivity (VII), % mass Productivity by total raw material, % mass Temperature,
°C Pressure,
MPa Time,
min Raw material productivity (II), wt % from (I) Recirculation ratio, (II/I) Temperature,
°С Pressure,
MPa Time,
min BUT AT FROM (I) B+C 20÷80 120÷180 410h
500 1.2h
2.5 30÷90 180÷300 1.8÷3.0 450h
500 0.3h
0.5 2160h
2880 ≥25.0 ≥5.0 one 60 thirty ten 100 100 fifty 150 410 1.4 60 250 2.5 480 0.4 2520 28.0 ≥5.5 2 60 thirty ten 100 100 fifty 150 480 1.4 60 250 2.5 480 0.4 2520 33.8 ≥5.5 3 60 thirty ten 100 100 fifty 150 440 1.2 60 250 2.5 480 0.4 2520 33.4 ≥5.5 four 60 thirty ten 100 100 fifty 150 440 2.2 60 250 2.5 480 0.4 2520 33.6 ≥5.5 5 60 thirty ten 100 100 fifty 150 440 1.4 thirty 250 2.5 480 0.4 2520 32.8 ≥5.5 6 60 thirty ten 100 100 fifty 150 440 1.4 90 250 2.5 480 0.4 2520 34.2 ≥5.5 7 60 thirty ten 100 100 fifty 150 440 1.4 60 180 1.8 480 0.4 2520 29.2 5.0 eight 60 thirty ten 100 100 fifty 150 440 1.4 60 280 2.8 480 0.4 2520 34.8 5.7 9 60 thirty ten 100 100 fifty 150 440 1.4 60 250 2.5 450 0.4 2520 32.6 5.0 ten 60 thirty ten 100 100 fifty 150 440 1.4 60 250 2.5 490 0.4 2520 32.6 ≥5.5 eleven 60 thirty ten 100 100 fifty 150 440 1.4 60 250 2.5 480 0.3 2520 32.8 ≥5.5 12 60 thirty ten 100 100 fifty 150 440 1.4 60 250 2.5 480 0.45 2520 33.3 5.5 13 60 thirty ten 100 100 fifty 150 440 1.4 60 250 2.5 480 0.4 2160 30.0 5.4 fourteen 60 thirty ten 100 100 fifty 150 440 1.4 60 250 2.5 480 0.4 2880 35.1 5.7

Claims (13)

1. A method for the production of petroleum needle coke by delayed coking, where at least three feedstock streams are used, one of which is highly aromatized, and the rest for less flavored feedstock, while all feedstock streams are derivatives of secondary oil refining products, in which less flavored feedstock streams are sent for heating and thermal polycondensation, after which it is sent to a distillation column, from the bottom of which the raw material is sent for coking with preheating, coking gas oil is returned to the distillation column, heavy gas oils from the distillation column are partially recycled for thermopolycondensation, and highly aromatic raw materials are sent for mixing to the flow at the outlet of the thermopolycondensation reactor in a ratio selected so that the temperature at the inlet to the distillation column does not exceed 350°C. 2. The method according to claim 1, in which the raw material is heated to 410-500°C before the thermopolycondensation reactor, and the thermopolycondensation is carried out at a temperature of 450-490°C for 30-90 minutes. 3. The method according to claim 1, in which the recirculation ratio is 1.8-3.0. 4. The method according to claim 1, in which the ratio of feedstock streams, namely: the first stream - low sulfur, decantoils of the catalytic cracking process (FCC) or heavy pyrolysis tars or coal tars and pitches, the second stream - low sulfur heavy residues of secondary processes, extracts oil production or heavy diesel fractions of catalytic cracking, the third stream - low-sulphur vacuum and atmospheric residues of oil distillation or sludge or petrolatum oil production, respectively, is 60/30/10 wt.%. 5. The method according to claim 1, in which the light components from the distillation column after cooling are removed from the plant as components of diesel fuels. 6. The method according to claim 1, in which the gaseous products are withdrawn from the top of the distillation column. 7. The method of claim 1, wherein the heavy gas oils from the distillation column are further partially recycled to the inlet of the distillation column. 8. The method according to claim 1, in which the raw mixture enters the contact devices of the separation section of the distillation column with a temperature of 300÷320°C. 9. The method according to claim 1, in which the coke chamber filled with coke is first steamed with water vapor, then the coke chamber is cooled with water, after which the coke is extracted, and for the duration of these processes, the supply of secondary raw materials is switched to a parallel coke chamber to ensure a continuous technological process . 10. The method according to claim 1, in which the number of coke chambers is at least two. 11. The method according to claim 1, in which the coking process proceeds at a temperature of 450-500°C, an overpressure of 0.3-0.5 MPa, for 32-48 hours. 12. Installation for the production of petroleum needle coke by delayed coking, which provides for at least three feedstock supplies, one of which is highly flavored, feed lines for less flavored feed streams are connected to the thermal polycondensation feedstock heating furnace, which is connected to the thermopolycondensation reactor, at the outlet of which the line the raw material supply is sent to the distillation column, from the bottom of the distillation column the technological line is sent to the coke chambers through the coking feedstock furnace, while the coke chamber is connected by the coking gas oil return line to the distillation column, the heavy gas oil output line from the distillation column is divided into the input to the thermal polycondensation feedstock heating furnace , to the inlet line to the distillation column and to the output as a product, and the highly aromatic feedstock is sent for mixing to the outlet stream from the thermopolycondensation reactor to the supply line to the distillation column nu. 13. The apparatus of claim 12, wherein a cooling device is provided in the recycle heavy gas oil supply line to the distillation column inlet line.

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