SU1087077A3 - Process for preparing from petroleum processing residues of aliphatic type of carbonaceous material for use as sintering component in producing coke and aliphatic oil - Google Patents

Abstract

1391490 Making pitch KUREHA KAGAKU KOGYO KK 28 March 1972 [1 April 1971] 14561/72 Heading C5E A high aromatic pitch for binding with a weakly coking coal is made from a petroleum base residual oil containing alpihatic hydrocarbons by heating the oil to a temperature in the range 300‹ to 500‹ C. by direct contact with a non-oxidizing gas which is at 400‹ to 2000‹ C. and maintaining the temperature, optionally with the aid of external heating means for from 0À5 to 20 hours, to effect cracking, polycondensation and aromatization reactions. Suitable oils include vacuum residuals, catalyzed and non-catalyzed thermal residuals, duo-sol extracts residues, furfural extracts, propane extraction residues and hydroformer residuals, and' the pitch has a softening point in the range 130‹to 300‹ C., fixed carbon content of from 40% to 80% b.w., and an H : C atomic ratio in the range 0À4 to 1À1. The non-oxidizing gas may be N 2 , A, steam, H 2 , hydrocarbon gas or a totally combusted gas, and a preheating stage may be combined with this method, e.g. the oil being heated to 350‹ to 600‹ C. by external heating means for from 0À5 to 60 minutes at from 0 to 150 kg./cm.<SP>2</SP> gauge. Product H 2 or light oils from the second stage may be recycled to the preheating stage to inhibit coking there and reduce the sulphur content of the pitch product.

Description

The invention relates to a method for producing carbon-containing material from an aliphatic type of petroleum residue; used as a sintering component in a coal mixture to obtain coke and aliphatic oil. At present, coke and foundry furnaces are produced from coal that has high coking coal. properties.  However, due to the ever-lower availability of highly coking coal sources, attempts are made to use weakly coking coals as a source material for producing coke in combination with a binder.  The use of coal-based pitch or petroleum-based solid pitch is known.  However, coal pitch cannot satisfy the industrial demand for this product due to a quantitative reduction of such a source. On the other hand, petroleum tar pitch cannot be used as a binder because it is not suitable for mixing with coal because of its chemical composition, in which the main components are synthetic and hydrocarbons, in addition to its low yield during carbonization.  As a result of research aimed at studying the bonds suitable for lightly coking coals in the production of coke used for blast furnaces or in the foundry industry, it has been found that a petroleum-based carbon-containing material (pitch) is well suited for use as a binder. of the type described, can be obtained by heat treatment of the bottom residue. on the basis of oil, in this case, an efficient flow of cracking, polycondensation and aromatization reactions is provided, and this bottoms residue consists mainly of aliphatic hydrocarbons.  The aim of the invention is to create a material. suitable for use as a binder, which provides a high coking behavior for low carbon and, besides creating a process suitable for the production of such a material on the basis of oil.  The goal is achieved according to the method of obtaining from alfatic type oil refining the carbonaceous material used as a sintering component in the coal charge to obtain coke, and aliphatic oil, characterized by the fact that these oil residues are heated to 350-600 ° C under pressure ranging from normal pressure to 150 kgf / cm for 0.5-60 minutes in a tube furnace, then they are heated to ZBO-AZO C by contact with a non-oxidizing gas having a temperature of 400-2000 ° C to produce carbon dsoderzhaschego material having a softening temperature of 130-300 0 containing carbon-bonded 4080 wt. % and atomic ratio H / C of 0.4-1.1, and aliphatic oil with atomic ratio H / C of 1.55.  The softening point is measured using a Kok type flow tester, in which 1 g of the sample is loaded into a cylinder with an internal diameter of 10 mm, having a nozzle with a diameter of 1 mm at one end, and then heated at a rate of 1 minute under load c. 10 kg / mm to determine the temperature at which flow through the nozzle begins.  The amount of bound carbon is determined by | UT in accordance with Japanese Standard JIS-K-2421/1906 /, and the atomic ratio H / C is obtained in accordance with elementary analysis.  A carbon-containing material characterized by these properties can be obtained by transforming the chemical structure and composition of the original petroleum sludge residue by heat treatment and is replete with aromatic constituents, providing good mixing with coal and high carbonation yield.  Consequently, the proposed material (pitch), when using low-coking coals, provides improved bonding forces and co. Moreover, coke based on it has a high strength comparable to that of coke produced from well-coking coal.  The mixing ratio of the proposed pitch with lightly coking coal varies depending on the coal used.  For example a mixture of 50 wt. h  lightly coking coal (Newdell) n 50 wt. h  the proposed pitch provides coke strengths of the order of 91.4, and a mixture of 40 wt. h  coking coal of Australia, 40 wt. H low carbon from Japan, 20 wt. h  highly coking coal from the USA and 1 wt. h  the proposed pitch provides the strength of coke 91.5.  In addition, the use of the proposed pitch in combination with coal, which in itself has low coke strength, gives coke, which is well comparable in quality to coke obtained from highly coking coal (bituminous coal).  During the heat treatment of the petroleum bottoms residue according to the invention, cracking reactions and polycondensation as well as aromatization reactions take place, and this bottoms residue contains aliphatic hydrocarbons. bottom residue of thermal cracking, bottom residue of catalytic thermal cracking, t. e.  vat residues, such as those obtained in conventional oil refining industry.  and various varieties of bottoms, such as Duoso extracts, furfural extracts, propane extraction residue, distillation residues of catalytic dehydrogenation, and mixtures thereof.  However, from an economic point of view, vat residues containing more than 30% by weight are not preferred. % fraction having a boiling point not higher.  Thus, as source materials, bottoms that exist in a verd or semi-solid state at room temperature are preferred, similar to the bottom residue of vacuum distillation.  Such oil bottoms are used as a fuel or as a material for asphalting roads.  However, most oil bottoms have a high sulfur content, so that they create significant problems associated with environmental pollution due to the formation of sulfur dioxide that occurs when used as a fuel.  Therefore, the use of such bottoms as fuel should be strictly limited.  The need for road asphalting materials is now steadily increasing.  However, the supply and production rates of bottoms associated with an increase in the production of petroleum products or petrochemicals significantly exceed the demand for bottoms for such purposes, therefore a serious problem is expected in the future that will hinder the growth of refining industry.  Due to the significant shortage of well-coking coals for use in blast furnaces, repeated attempts have been made to obtain artificial coking coal from oil bottoms to produce coal substitutes with high coke strength.  These products create many obstacles to practical use due to excessive sulfur content and high cost.  The proposed pitch has significant advantages in economics and in terms of sources of materials, while it is produced by transforming the structure or composition of the bottoms such as petroleum asphalt.  The advantages of the proposed binder are that coke for use in a blast furnace of high quality can be produced by adding a small amount of the proposed pitch to the usual coal mixture used in a blast furnace.  At the same time, significant savings are expected in the use of well-coking coal, which is expensive and difficult to access due to the exhaustion of its sources, and it is possible to produce high-quality coke.  In addition, non-coking or weakly coking COAL can be turned into high-quality coal with high coking properties by adding the proposed pitch.  The various conditions required for the heat treatment of the raw materials in accordance with the invention are chosen in such a way as to ensure the production of a pakoprodukt having the specified properties.  The heat treatment process for producing the proposed pitch is as follows.  Vat residue on the basis of oil containing aliphatic hydrocarbons,.  is heated to ZZO-BOO C under a pressure of 0-150 kg / cm for 0.560 minutes and then brought into direct contact with a non-oxidizing gas heated to AOO2000 ° C, keeping the residue at a temperature below. than with a carrier gas, but not more than, in order to complete the heat treatment. Then, an oil-based vat residue containing aliphatic hydrocarbons is heated and maintained at a temperature in the range from 300 to 500 ° C under pressure from 0 to 150 kg / cm for 0.5-20 hours using heat from the outside.  Used for such heat treatment. apparatuses are referred to as internal and external heating systems, or to systems with combined heating, and these systems are further classified as single-stage and multi-stage.  In the case of an internal heating system, nitrogen, argon, steam, hydrogen, a hydrocarbon gas, or a completely burnable gas, such as a non-oxidizing gas, are used as the coolant.  This heat carrier is heated / melted to a temperature in the range of 4UU2000 C, and then brought into direct contact with the initial residue.  In this regard, to achieve smooth thermal cracking and aromatization and polycondensation reactions, as well as to prevent local overheating by the coolant, it is necessary to maintain the original residue at a temperature below the coolant temperature, but not more than, in most cases in the range from 300 to 500 ° C, preferably from 380 to 450 ° C.  In the alternative, however, the initial residue molset will be temporarily heated prior to the preheating stage and allow for partial cracking if it occurs.  There are no restrictions for the process to bring the heat transfer gas into direct contact with the original residue.  It is possible to introduce heat carrier gas into the initial residue, or to use a jet scrubber, which ensures efficient mixing of gas and liquid, and so on. P.  This reaction can be carried out for individual batches and continuously.  The essence of this process is to convert the residue into a lek with the desired properties using the following operations.  The desired thermal cracking is carried out for a short period of time by bringing the heat carrier gas at direct temperature into direct contact with a large amount of the original residue.  (The remaining mass of the original residue serves to prevent local overheating).  A portion of the original bottoms residue that is unstable at elevated temperatures is separated or gasified to be removed from it.  A portion of the initial residue, relatively stable with respect to heat, is maintained at a temperature that is significant, but not harsh, for the residue, for a relatively long period of time in order to carry out polycondensation and aromatization reactions.  So dl. The greatest advantages are obtained by using the difference in the thermal behavior of the materials contained in the initial residue, which has a complex chemical composition and a complex structure.  In accordance with the proposed process, the initial cubic residue with some specific weight can be eff. )) is processed by heat carrier, | {using less thermal energy than in the case of conventional thermal cracking in an internal heating furnace, for example, thermal energy having about one-tenth of the energy required for such a common case. .  This is due to the fact that the thermal energy introduced by the coolant into the system causes the thermal cracking of the initial residue, while the free radicals serve as an initiator of polycondensation reactions and aromatization of molecules in the liquid phase. This allows the reactions to flow smoothly the liquid phase at temperatures that are not too hard for the original residue, and contributes to /: -. tilting produced oils.  The specified conditions are found in. a result of experiments based on the aforementioned reference points of view. The lower temperature limit for the gas carrier or for the original residue is intended. to determine the smooth flow conditions for these reactions, while the upper limit for the temperature of the heat transfer gas and the initial residue is given in order to prevent undesirable effects of coking.  The intensity of the heat carrier gas flow can be chosen arbitrarily as a function of temperature conditions.  If such conditions are properly regulated, then distilled oils and residual pitch can be adjusted to provide a certain structure and composition.  The pressure in the reactive system is chosen near normal.  However, the reaction may i-take place, and vice versa, by changing the indicated pressure range, for example, from 15 kg / cm, preferably from 0.95 to 6 kg / cm (from the excess).  On the other hand, either a reflux type cooling device or a circulation type cooling device is used to prevent the initial residue from overheating.  Conversely, the internal temperature can be maintained at a predetermined interval due to additional heating from the outside.  The drawing shows an installation diagram for carrying out the proposed method on an industrial scale.  The installation comprises a reservoir 1 for storing the initial residue, a pump 2, a cracking preheating furnace 3, a valve 4, a reactor 5 and a separation column 6.  The installation works as follows.  The original bottoms from the tank 1 of the original residue are fed by means of a pump 2 to the cracking 1 8 l 3 to provide preheating and primary cracking.  This is a tubular type furnace using a conventional external heating system.  In order to prevent coke formation in the heating tube and to reduce the sulfur content in the pection products, hydrogen or light hydrocarbons can be introduced, such as being part of the light oil produced in the process according to the invention.  The conditions for said thermal cracking vary depending on the presence or absence of introducing gases, such as hydrogen, as well as on the secondary reaction stage.  However, the temperature used should preferably be in the range from 350 to, the pressure in the range from normal pressure to 150 kg / cm, and the residence time in the range from 0.5 to 60 minutes.  Valve 4 serves to regulate pressure in the preheating stage.  The initial residue, which is subjected to primary pre-cracking or heating, is then introduced into reactor 5, where secondary cracking and separation of lighter fractions (gas, oils) resulting from cracking takes place.  The reactor 5 is equipped with a nozzle 7, through which the heat-transfer gas is introduced at an elevated temperature as a heating source, as well as a carrier for the distilled substance at the moment of release.  The secondary cracking conditions depend on the primary cracking conditions during preheating.  However, the temperature used should be in the range from 300 to, as mentioned, preferably in the range from 380 to, pressure in the range from 0.98 to 15 kg / cm (excess), preferably from 0.95 to 6 kg / cm, and stay in the range from 0.5 to 20 hours, preferably from 0.5 to 10 hours  The cracked gaseous and liquid products, which are separated during the reaction, are introduced via line 8 into the cooling separation column 6, so that gas 9, light oils 10 and bottom residue 11 are separated and withdrawn in the usual way.  The pitch that was produced in the reactor 5 is fed through line 12 through valve 13 to cooling tape 14 for curing and is obtained as pec-products.  Valve 13 is designed to control the level of the liquid (reaction time) in the reactor 5. Systems with external heating can be divided into processing at the preheating stage and secondary heat treatment to complete the reaction. The use of a tubular heater as described is advantageous in terms of efficiency and also to provide acceptable reaction rates.  Although the necessary reactions can be carried out. only during the flow through the tubular heater, is the reaction also carried out using a reaction cube.  Delayed coking devices are used in these cases. Gaseous or oily by-products obtained during the process can be separated using various methods of distillation. The properties of the pitch in accordance with the invention should be as follows: with an atomic ratio H / C above 1, 1, the compatibility with coal is observed to be unsatisfactory, while with a lower H / C ratio, the binding force is reduced due to the increased content of the component having a lower smoothness.  When the softening point is too low, it becomes difficult to grind the pitch and store it without block formation.  Conversely, a too high softening current leads to an increased content of components having a low melting point, thereby resulting in reduced compatibility with coal.  If the content of bound carbon is too low, then increased evaporation occurs, thereby hindering the production of coke having a high density and strength.  If the content of bound carbon is too high, then this leads to a decrease in the binding force due to an increase in the number of components having a low melting point.  Thus, the essence of the invention is to create a process for the production of pitch using operations that transform the chemical structure and composition of the bottoms.  produced as by-products in the petrochemical industry, thereby improving mixing ability with coal and yield, which is suitable for use as a binder in the production of coke used in the foundry industry and in blast furnaces.  In addition, the proposed pitch may find other applications, for example, as a binder for the production of graphite products and refractories.  The oily substances produced during the production of the proposed pitch consist essentially of paraffinic hydrocarbons, which are used not only as lubricating oils, but are also valuable products for use in the production of gasoline or petrochemicals.  These oily products are well suited for use as fuel or fuel additives because of their low sulfur content and are therefore preferable from the point of view of environmental protection requirements.  In thermal cracking, as it is carried out in the proposed process, most of the sulfur contained in the original bottoms is separated and removed as a gas.  On the other hand, although some sulfur may be contained in distilled oil, such sulfur can be easily isolated and removed using a conventional desulfurization process.  Thus, the proposed process is not only an effective method for producing sulfur, but also provides improved quality of distilled oils.  Example 1  6kg of bottoms from the vacuum distillation of crude oil from the Khafji field is loaded into a reaction tank equipped with a stirrer, a heater and a cooler.  Then the heat transfer gas is preheated to.  high temperature, injected through a nozzle having an inner diameter of 15 mm, into the residue and maintained at a constant temperature for a predetermined period of time.  The bottoms of the vacuum distillation of crude oil from Kafji Field 111 is characterized by the following properties: specific gravity 1.032; bound carbon 12.8 wt. %; the point of softening is 46 ° С; ash content 0.05 wt. %; boiling point.  This residue contains cubes, weight. %: C 84.0; H 10.41; N 0.66; S 4.90; H / C 1.49.  In tab.  Table 1 presents the conditions for conducting the process, and Table 2 shows the material balance.  The results of this test show that a highly efficient use of thermal energy is being achieved. The properties of the distilled oil and the obtained pitch are given in Table.  3 and 4 respectively.  In tab.  5 shows the results of a sintering test for determining the coking ability of a pitch for a blast furnace.  This test was carried out on the pitch obtained in Test 1.  The sintering test is as follows: 18-liter oil barrels are loaded with samples having the same granule size as in real conditions, and placed together with another load into a coke oven of industrial scale for the purpose of coking, with the side walls of the barrel supplied holes.  The results are shown in Table.  5 show that the proposed pitch provides excellent properties as a binder.  An elementary analysis of distilled oils from experiments 1 was carried out and NMR and IR spectra were taken.  These tests show that the oils contain from 60 to 80% aliphatic hydrocarbons.  The strength of mixtures containing pitch 2 and 3, mixed in the same proportion as for 3, is 92 in any case. Example 2.  Distillation distillation at normal pressure at 350 ° C from Arabic light crude oil, the properties of which are given in Table 6, is loaded into the device used in Example 1.  The properties of the bottoms obtained by distillation under normal pressure of Arabic light oil are as follows: Specific gravity 0.957 Residual carbon 10.2 Softening point Below room temperature 12 Ash content, wt. % 0.03 Elementary analysis, weight. % С84.9 Н11.67 N0.14 S3.39 N / С1.65 As a result of operation under the conditions described below :.  Gas coolant Nitrogen.  Heat carrier temperature, ° G 700 Heat flow intensity, m3 / h5.0 Initial residue temperature, ° С430 Duration of work, min120 consider the following physical bass, weight. %: Sc.  Hydrocarbons H2S Distilled Peck Oil Loss The properties of the image obtained in this way are as follows: Specific gravity () 0.920 Splash point 184 Distant thermal test, ° C Distilled,% 13 Softener, C Bonded carbon, wt. % Ash, weight. % Elementary analysis, weight, C 85.9 6.61 0.49 6.54 0.92 The resulting pitch is subjected to a sintering test, as was used to produce coke in the same proportions as in Test 3 in Table.  five.  The coke strength obtained is 91.  Get distilled oil of the following composition, wt. %: Example 3.  The bottoms of the vacuum distillation of crude oil from the Khafji field, preheaters heated to 350 ° C, are heat treated in a tubular heater at a maximum temperature of 475 C for 13 minutes.  Then, the bottom residue treated in this way was taken to a bottom at a normal pressure, so that about half of the bottom of the rest of the tank was distilled off as a liquid with a yield of 45% by weight. % of t.og Properties of initial heavy oil.  The following: H / C ratio 1.49.  Specific gravity1.032 The softening point, ° С 46 Ash content, weight. % 0.05 7714 Initial distillation temperature at normal pressure C The properties of the resulting pekoprodukt are listed below: Softening point, ° C 130 Bound carbon, wt. % 42 Insoluble in benzene substance, wt. % 10 Insoluble in quinine substance, weight. % O The H / C1.08 ratio of Peck, derived from a heavy oil based on petroleum and consisting essentially of aliphatic hydrocarbons, exhibits properties similar to those of coal asphalt pitch, consisting mainly of aromatic hydrocarbons.  The pitch thus obtained is ground to powder and mixed with various grades of coal, then the prepared mixture is subjected to a sintering test, as used in the production of coke for blast furnaces.  In tab.  6 shows the results of such a test, demonstrating the excellent properties of the produced coke.  Example 4  The bottoms residue of vacuum distillation of Iranian heavy sulfur oil, preheated to 350 ° C, is heated to 410420 ° C in a tubular heater and then introduced into the reaction cube and held for 12 hours.  During this operation, the cube is maintained under a pressure of 5 kg / cm (excess), and the loaded residue is maintained at 410-420 C.  Then, steam at l 200 ° C is introduced into the cube to remove a fraction of the light oils from it with a net yield of 32% by weight of heavy pitch as a residue based on the weight of the initial residue.  The same operations were carried out as in example 3, in particular under the same conditions as in the conditions indicated in columns 2, 4 and 5 in the table.  6 for testing as carried out in the production of coke for blast furnaces.  The strength of coke products is 91.6, 89.2 and 91.4.  The following are the properties of the resulting bake:

15 size point,

Fixed carbon

weight 7o

Insoluble in

benzene substance

weight.%

Insoluble in

quinoline substance

weight;%

Ratio H / G Example 5. A pitch obtained analogously to example 3 was placed in a maturation cube, equipped with a stirrer, for heat treatment. This heat treatment is carried out at normal pressure at 400-410 0 for 6 hours. Light oils formed during the heat treatment are removed by distillation, and heavy, highly aromatized pitch is obtained with a yield of 59% by weight (26.5% by weight (% based on the weight of the initial residue) The resulting pitch is characterized by the following properties: the softening point of the benzene insoluble substance is 65%; quinoline insoluble substance 38%; I / C ratio 0.76 and 60% bound carbon This peck was tested for coking ability as a coking binder under the same conditions as in experiments 2, 4 and 5 in the table. 6, with good results giving coke strengths of 91.8, 81.1 and 92.3 respectively. Conducts tests for pitch as a binder of the following composition: Weak coal from Australia (Nyodall),% 70-50 Suggested pitch,% 30 50 Coke strength 88.7 91.4 It turned out that the mixture of low-carbon coal from Australia (Nude with the proposed pitch provides. coking ability comparable to coking ability C of hard coking coal.

707716

Example 6. When using the bottom residue vacuum distillation of the same material as at Step 1, the initial residue residue was tested at about 100 kg / h, and the device shown in the drawing was used;

10 Superheated steam is introduced as a heated coolant at a flow rate of 30.4 kg / h. The test conditions are as follows: T (temperature at the outlet of the preheating furnace with cracking) 480 ° C; T. (temperature inside the reaction cube) PQ (pressure at the inlet of the preliminary cracking heating furnace 32 kg / cm (g); P (pressure at the exit of the preliminary cracking heating furnace) 10 kg / cm (g); (pressure inside the reaction cube) 0, 1 kg / cm (g); 0 (residence time in the preliminary cracking heating furnace) 3.2 h; 02 (residence time inside the reaction cube) 3.5 h. The following products are obtained, wt.%: Gas 4.6; light oil P, 3; heavy oil 48.4 and residual pitch 25.5.The properties of the obtained products are shown in Table 7. Table 8 shows the result tests considered in the light of the above conditions of temperature and pressure (Experiment 1 was proposed). Following this, the pitch obtained during each of these tests P1I was subjected to a coking test. The mixture used in this test consisted of 80 parts by weight. U.S. coal from the USSR, which is the Nexux osh, ei coal, and 20 parts by weight of pitch.Table 8 shows that the products obtained in each case provide a quality comparable to the quality resulting from the use of well-coking coal.

17

1087077

18 Table 1

Temperature of heat carrier gas, ° С

Gas flow rate1500

500

700

Table 2

Specific gravity Point of the flashes, From the start of the distillation,

20% distilled

50% distilled

80% distilled Elemental analysis, wt.%

WITH

H

N

S

s / s Note. ..

0,940

0.934

152

146

200

211

344

331

460

474

520

525

84.80

85,6

11.88

12.15

0.43

0.36

2.32

2.26

1.71

1.68 The stated temperatures are recalculated to boiling points (° C) at normal pressure. .Table4 Properties of pitch:, J N.%. S,% H / C Insoluble in benzene, wt.% Insoluble in quinoline, wt.% These figures were obtained using a melting device manufactured by Yanag Kyoto, Japan. Components of the mixture,% Coking coal from the USA (volatile matter 19-20%). 20 Coking coal from Australia (volatile matter 20-23%). 40 Low-coking coal from Japan (volatile matter 35-40%) 40 Proposed pitch from experiment 1 Drum index 92 for 1

40 Continued table. 4 Experience 111 1 1,901,761,56 6,084,754,48 0,650 0,7520,786 65,474,858.9 32,040,327.2 for determining points of Micro-Moto BusinessSurgery Company, Table 5 Comparison experience Suggested 23.4 5 - 10 50 40 45 504545 -51015 76939193

Hard coal from USA

(volatile matter 18-19%)

Coking coal from australia

(volatile matter 26-28 wt.%)

Low grade coke from Japan

(volatile matter 35-40 wt.%)

Peck according to the invention

Coke strength

11.9

C 7.4

n

32.5 2.7

Boiling point

20%

15.6 80% 7.5

10.7 11.6

O10

50

50.45

5045

50

055 82.2 88.3 90.8

Table 7

87.7

83.5

3.5

From 5.77

11.4

14.6

H 6.15

4.6

1.6

8С

N / S 0.78

212 Associated C 67.0 325

20,505

Insoluble in benzene 58, 3

Insoluble in quinoline 27.0

Specific weight is 20C 1.25

25

The amount of the supplied initial residue, kg / h

The amount of fluid introduced

at elevated temperature, kg / h

The temperature of the coolant, entered at povipinoy temperature, with

Temperature at the exit of the preliminary cracking heating furnace, С

The pressure at the outlet of the furnace pre-cracking heating, kg / cm

Pressure at the inlet of the preliminary cracking heating furnace, kg / cm

Residence time in the pre-cracking heating furnace, min

The temperature of the liquid in the reaction cube, ° C

Liquid pressure in the reaction cube (P) i kg / cm (g)

Average residence time in the reaction cube, h

Product yield, wt.% Gas

Light oil T Yellow oil Residual pitch Softening temperature of pitch, St carbon, wt.% Insoluble in benzene,%

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26 Table

100 102 100 103

50.7 25.0 18.5 5.3

620 850 850 1600

380 475 485 480 Properties of the pitch ° С 230 218241232229 58,369,366,268.4 67.0 0.820,770,780.71 49,259,558,663,2

27

Insoluble in quinoline. Coking ability (5)

The coking ability in the case of only one OS coal is equal to 15.1.

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28 Continuation of table. eight

pitch 14.0 29.1 26.1

30.3 g 91.7 93.1 92.4

92.1

Claims (1)

METHOD FOR PRODUCING FROM RESIDUES FROM REFINING OIL OF ALIPHATIC TYPE OF CARBON-CONTAINING MATERIAL USED AS A SINTER- A QUALIFIED COMPONENT IN A COAL MIXTURE FOR PRODUCING COX, AND ALIPHATIC OIL, characterized in that said oil residues are heated to 350-600 ° C under pressure ranging from normal pressure to 150 kgf / cm ² for 0.5-60 minutes in a tubular furnace, then they are heated to 380-450 ° C by contact with a non-oxidizing gas having a temperature of 400-2000 ° C to obtain a carbon-containing material having a softening temperature of 130-300 ° C, containing a bound carbon of 4080 wt.% and an atomic ratio of N / C 0.4-1.1, and aliphatic oil with § atomic ratio Niemi H / C of more than 1.55. about SU ", 1087077