KR101658181B1 - Hydrogen donor, method for manufacturing additives using the same and method for manufacturing cokes using the same - Google Patents

Abstract

The present invention relates to a hydrogen donor, a method for producing an additive using the same, and a method for preparing a coke using the same. More particularly, the present invention relates to a hydrogen donor used as an additive capable of improving the strength of a coke added to coke, A method of manufacturing an additive using the same, and a method of manufacturing a coke using the same.
A method for manufacturing an additive according to an embodiment of the present invention is a method for producing an additive to be added to coke for coke production, comprising the steps of: preparing coal; A process of preparing hydrogenated tar; Mixing the coal and hydrogenated tar; Modifying a mixture of coal and hydrogenated tar; Separating the liquid phase of the modified mixture; And recovering the solute from the liquid phase of the modified mixture.

Description

FIELD OF THE INVENTION [0001] The present invention relates to a hydrogen donor, a method for producing an additive using the same, and a method for producing a coke using the same. BACKGROUND ART [0002]

The present invention relates to a hydrogen donor, a method for producing an additive using the same, and a method for preparing a coke using the same. More particularly, the present invention relates to a hydrogen donor used as an additive capable of improving the strength of a coke added to coke, A method of manufacturing an additive using the same, and a method of manufacturing a coke using the same.

Coal, which is usually used to make coke, is classified as hard coal and untreated coal depending on the degree of cohesion.

In order to produce coke of high strength, it is advantageous to use strong coals excellent in the degree of cohesion or to use a large amount of strong coals compared with uncoated coals, and thus strong coals have been used in large quantities in the production of coke. However, due to the rapid increase in demand for coking coal for metallurgical use globally and the limited reserves of hard-boiled coals, it has become increasingly difficult to secure strong coals, which has led to a surge in prices. Therefore, although the amount of tin coals to be used must be increased in order to reduce coke manufacturing costs, the quality of the coke is deteriorated due to the lack of the point resistance of the tin coals.

Therefore, a method of improving the degree of cohesion by mixing an additive to a coking coal (or a combination carbon) containing a large amount of untreated carbon has been used. Methods for producing additive for securing the cohesiveness of tinned carbons include a method of extracting a tacky component contained in coal with an organic solvent and a method of adding a cohesive substance by donating hydrogen to a non- And the like.

The method of producing additive by modifying the coal in the same manner as in the coal liquefaction process produces an additive at a higher temperature and pressure condition but has a complex reforming process and it is difficult to carry out a reaction process in which donor have. In addition, expensive hydrogen chemicals should be used continuously when donating hydrogen to modify non-cohesive materials. Therefore, the increase in the amount of the chemical agent that can be caused by deterioration, denaturation, leakage, incomplete recycling, etc. of the hydrogen donor characteristic is the biggest factor that lowers the economical efficiency in commercializing the coal reforming process. The development of new economic alternative materials that can donate to the market has become very important.

KR 10-0866166 B1 KR 10-1418053 B1

The present invention provides a hydrogen donor which is easy to manufacture, a method for producing an additive using the same, and a method for producing coke using the same.

Also, the present invention relates to a hydrogen donor which can improve the yield of an additive by modifying a tinctorial amide to improve the yield of the additive, economically replace the expensive chemical agent used at the time of modification, thereby saving manufacturing cost, and A method for producing an additive, and a method for producing a coke using the same.

The hydrogen donor according to the embodiment of the present invention is a hydrogen donor used in the preparation of an additive to be added to coke for the production of coke, which is obtained by adding hydrogen to tar produced at the time of carbonization of coal, The content of aliphatic carbon in the total carbon is larger than the content of aromatic carbon.

The aliphatic carbon and the aromatic carbon may be contained in a ratio of 1: 0.35 to 1: 0.40.

Wherein the hydrogen donor has a boiling point of 200 to 230 DEG C for distilling 10 wt% of the solution, a boiling point of 285 to 300 DEG C for distilling 50 wt% of the solution, and a boiling point of 90 wt% The temperature may be between 330 캜 and 360 캜.

Also, a method for producing an additive according to an embodiment of the present invention is a method for producing an additive to be added to a coke for coke making, comprising the steps of: preparing coal; A process of preparing hydrogenated tar; Mixing the coal and hydrogenated tar; Modifying a mixture of coal and hydrogenated tar; Separating the liquid phase of the modified mixture; And recovering the solute from the liquid phase of the modified mixture.

The process for preparing the hydrogenated tar may be carried out by adding hydrogen to tar generated at the time of coal carbonization.

The hydrogenated tar may include aromatic carbon to aliphatic carbon in a ratio of 1: 0.35 to 1: 0.40.

The boiling point for distilling 10 wt% of the hydrogenated tar is 200 to 230 DEG C, the boiling point for distilling 50 wt% is 285 to 300 DEG C, the boiling point for distilling 90 wt% Lt; RTI ID = 0.0 > 330 C < / RTI >

The step of modifying the mixture of coal and hydrogenated tar may include a step of reacting the mixture in a reaction vessel having a temperature of 300 ° C to 500 ° C and a pressure of 60 bar to 80 bar for 40 minutes or more.

And separating the non-volatile oil component from the liquid phase of the modified mixture prior to recovering the dissolved component from the liquid phase of the modified mixture.

The step of separating the oil component may include a step of heating the liquid mixture of the modified mixture to a temperature above the boiling point of the oil component to separate the oil component from the dissolved component.

The step of separating the oil component may include a step of heating the liquid phase of the modified mixture to a temperature of 350 ° C to 450 ° C to separate an oil component having a boiling point of less than 350 ° C to 450 ° C from the dissolved component .

The coal for the additive production may contain unfired coal.

In addition, the method of manufacturing coke according to the embodiment of the present invention mixes the additive prepared by the above-mentioned method with coke to produce coke.

According to the hydrogen donor, the method for producing the additive using the same, and the method for producing coke using the hydrogen donor according to the embodiment of the present invention, high strength coke can be manufactured using coal, especially, a resource that is rich in resources and low in cost. Therefore, it is possible to increase the content of unreacted carbon contained in the coking coal, and thus it is possible to economically provide the coke of good quality even when the demand for the coking coal for metallurgy is increased.

In addition, it is possible to economically substitute expensive chemical agents used in the production of additive while ensuring the integrity of the additive, thereby improving the stability of the operation in accordance with the process simplification, and solving the environmental problem caused by the increase in use of chemical agents.

In addition, the additive can be greatly improved by producing the additive by the method of modifying the unreacted carbon, and the additive can be additionally produced as a by-product.

1 is a block diagram schematically illustrating an additive manufacturing facility according to an embodiment of the present invention;
2 is a graph showing ¹³ C-NMR spectra of hydrogenated tar according to an embodiment of the present invention.
3 is a graph showing the results of simulated distillation analysis of hydrotreated tar according to an embodiment of the present invention.
4 is a flow diagram illustrating a method of manufacturing an additive in accordance with an embodiment of the present invention.
5 is a block diagram showing a coke making method according to an embodiment of the present invention.

The hydrogen donor according to the present invention, the method for producing the additive using the same, and the method for producing coke using the same, are presented in the technical features of improving the strength of the coke by being added to the coke.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. The present invention may, however, be embodied in many different forms and should not be construed as being limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, Is provided to fully inform the user. Wherein like reference numerals refer to like elements throughout.

The method of manufacturing an additive according to an embodiment of the present invention is a method of recovering an additive by modifying a non-clogging material of coal by hydrogen donating to a material having a clogging property, and is used for donating hydrogen to the non- Hydrogenated tar is used as a hydrogen donor to replace expensive chemical agents.

1 is a block diagram schematically showing an additive manufacturing facility according to an embodiment of the present invention. Referring to FIG. 1, an additive manufacturing facility according to an embodiment of the present invention includes a reforming reactor 100 for modifying a slurry mixed with triturating coal and hydrogenated tar under high temperature and high pressure, a reforming reactor 100 for mixing the reformed mixture with a solid component And a distillation apparatus 300 for separating the separated liquid components into fractions by fractional distillation into oil and additives.

Herein, unripe coal refers to coal having low or no cohesion and low price, such as low grade coal and low grade coal, and lignite, bituminous coal and the like can be used. A reforming reactor 100 for reforming the non-luminescent material into a material having a cohesive nature, a separation device 200 for separating the solid component and the liquid component of the modified mixture, and a distillation device 300 for recovering the additive from the separated liquid component ), An apparatus of a general constitution for producing an additive from the unexposed coal is used, and a detailed description thereof will be omitted.

Figure 2 is a graph showing the ¹³ C-NMR spectrum of the hydrogenated tar in accordance with an embodiment of the invention, Figure 3 is a graph showing the simulated distillation analysis of the hydrogenated tar in the embodiment; 2 and 3, the hydrogen donor according to an embodiment of the present invention is a hydrogen donor used in the preparation of an additive to be added to coke to produce coke, ≪ / RTI >

Hydrogenated tar used as a hydrogen donor generally refers to a substance in which hydrogen is added to a position where the tar generated at the carbonization of the coal is connected to a double or triple bond of carbon and carbon in the hydrogenation reactor. Generally, tar contains mostly aromatic carbon compounds. However, according to the embodiment of the present invention, hydrogen is added to a position where the hydrogenated tar is connected to a double or triple bond of carbon and carbon so that the content of aliphatic carbon in the total carbon contained in the hydrogenated tar is larger than the content of aromatic carbon do.

The hydrogenated tar according to the embodiment of the present invention may contain aromatic carbon in a proportion of 35% to 40%, preferably 37% to 38%, when the content of the aliphatic carbon in the hydrogenated tar is 100% . That is, as shown in the ¹³ C-NMR spectrum of FIG. 2, the hydrogenated tar used as a hydrogen donor according to an embodiment of the present invention may include aromatic carbon to aliphatic carbon in a ratio of 1: 0.372.

In addition, according to an embodiment of the present invention, the temperature of the boiling point for distilling 10 wt% of the hydrogenated tar has a range of 200 ° C to 230 ° C, and the boiling point for distilling 50wt% is 285 ° C to 300 ° C , And the temperature of the boiling point for distilling 90 wt% is in the range of 330 캜 to 360 캜.

Table 1 below shows the results of simulated distillation analysis of hydrogenated tar according to an embodiment of the present invention, and FIG. 3 is a graph showing the results of the simulated distillation analysis.

B.P. (占 폚) Fraction (wt%) 82.6 0 83.0 0.7 202.0 6.7 229.6 11.6 253.4 22.0 268.9 32.4 285.6 41.9 300.0 58.1 305.4 64.1 314.6 71.8 332.1 81.6 358.1 90.9 379.3 95.1 476.3 99.4

The tar is composed of a mixture of hydrocarbons and their derivatives, and has boiling characteristics as shown in Table 1 when the aromatic carbon to aliphatic carbon is contained in a ratio of 1: 0.35 to 1: 0.40. That is, as shown in Table 1, the hydrogenated tar distilled at a temperature of 82.6 ° C or lower at normal pressure is 0 wt%, and about 6.7 wt% to 11.6 wt% of the total hydrogenated tar is within a range of about 202.0 ° C. to 229.6 ° C. Distillation. Also, within the range of about 285.6 캜 to 300.0 캜, about 41.9% to 58.1% by weight of the total hydrogenated tar is distilled, and within the range of about 332.1 캜 to 358.1 캜, about 81.6% to 90.9% Weight percent is distilled.

That is, when hydrogen is added to tar generated at the time of carbonization of coal and the aromatic carbon is contained in a ratio of 1: 0.35 to 1: 0.40 relative to the aliphatic carbon, the hydrogenated tar has a distillation temperature of 10 wt% ° C., the distillation temperature of 50 wt% is 285 ° C. to 300 ° C., and the distillation temperature of 90 wt% is 330 ° C. to 360 ° C.

Therefore, the hydrogenated tar used as the hydrogen donor according to the embodiment of the present invention has a content of aromatic carbon and a boiling property with respect to the aliphatic carbon as described above in order to donate hydrogen to the non-luminescent material of coal, It is possible to replace expensive chemical agents such as tetralin. Comparison of the additive yield and G-factor in the case of using tetralin used as a hydrogen donor and hydrogenated tar as a hydrogen donor according to an embodiment of the present invention is related to the method for producing an additive according to the embodiment of the present invention Will be described in detail.

4 is a flow chart illustrating an additive manufacturing method according to an embodiment of the present invention. Referring to FIG. 4, an additive manufacturing method according to an embodiment of the present invention is a method for manufacturing an additive to be added to coke for coke making, comprising the steps of: preparing coal (S100); A process of preparing hydrogenated tar (S110); Mixing the coal and the hydrogenated tar (S120); A step (S130) of modifying a mixture of coal and hydrogenated tar; Separating the liquid phase of the modified mixture (S140); And recovering the solute from the liquid phase of the modified mixture (S150).

Here, the process (S100) for preparing coal and the process (S110) for preparing hydrogenated tar are not a time-series relation but may be performed independently or simultaneously.

In order to prepare an additive to be added to coke for coke production, coal is first prepared (S100). Here, the coal for making the additive has low or no cohesion and can be used at low cost, such as lignite, and bituminous coal. In the examples of the present invention, as a result of industrial analysis, untreated carbon having the components as shown in Table 2 below was used.

Bullet Industrial Analysis (%) moisture(%) VM Ash FC Tie-in shot 45.0 9.6 45.5 12.7

On the other hand, the hydrogenated tar to be mixed with the unexposed coal is prepared (S110). As described above, hydrogenated tar generally refers to a substance in which hydrogen is added to a position where tar formed during carbonization of coal is connected to a double or triple bond of carbon and carbon in a hydrogenation reactor.

When the content of the aliphatic carbon in the hydrogenated tar is 100%, the aromatic hydrocarbons may be contained in an amount of 35% to 40%, preferably 37% to 38%, of the aromatic hydrocarbons, % Of the boiling point for distillation is in the range of 200 ° C to 230 ° C, the temperature of boiling point for distilling 50wt% is in the range of 285 ° C to 300 ° C and the boiling point temperature for distilling 90wt% Lt; RTI ID = 0.0 > 330 C < / RTI > to < RTI ID = 0.0 > 360 C. < / RTI >

As described above, when unreacted carbon and hydrogenated tar are prepared, slurry is prepared by mixing the uncharged carbon and the hydrogenated tar (S120). The slurry was crushed to have a particle size of 0.1 mm or less for the preparation of the slurry, and the crushed unbaked coal and the hydrogenated tar were uniformly mixed at a weight ratio of 1: 2 to prepare a slurry do.

Thereafter, the mixed mixture of the tantalum carbide and the hydrogenated tar is supplied to the reaction vessel, that is, the reforming reactor 100, and is reformed into a material having a cohesive property (S130). At this time, the process of modifying the mixture of the unreacted carbon and the hydrogenated tar is performed by reacting the mixture in the reforming reactor 100 having a temperature of 300 ° C. to 500 ° C. and a pressure of 60 bar to 80 bar for 40 minutes or more . In the embodiment of the present invention, the mixture obtained by mixing the unreacted carbon and the hydrogenated tar was subjected to a reforming reaction in the reforming reactor 100 having a temperature of about 400 ° C and a pressure of about 70 bar for about 45 minutes. Here, the reforming reactor 100 for reforming the non-luminescent material into a material having a cohesive nature uses a device having a general structure used in an additive manufacturing process, and a detailed description thereof will be omitted.

Also, according to the embodiment of the present invention, the mixture of the unreacted carbon and the hydrogenated tar is reformed in the reforming reactor 100, and then the temperature and the pressure of the reforming reactor 100 are maintained at a temperature of 100 ° C or less And a pressure of 20 bar or less. This is to terminate the reforming reaction quickly, and then the reformed mixture is sufficiently cooled at normal temperature and atmospheric pressure.

As described above, the mixture cooled at room temperature and normal pressure exists in a state where a solid component and a liquid component are mixed. Accordingly, the mixture is divided into a solid component and a liquid component in the separation device 200 (S140). The separated solid component can be used for various fuels, and the liquid component is recovered as an additive and its by-product oil.

That is, the liquid component has a component having a cohesive property and a component having no cohesion, and the component having no cohesion is an oil having a low molecular weight, and has a boiling point lower than 350 캜 to 450 캜. Thus, the fractional distillation process can be used to separate non-cohesive oil components from liquid components.

To this end, the liquid component of the mixture sufficiently cooled to room temperature and atmospheric pressure is heated in the distillation apparatus 300 to a temperature of 350 ° C to 450 ° C at a temperature above the boiling point of the oil component, that is, at normal pressure. At this time, since the boiling point of the oil component having no cohesion is lower than 350 ° C to 450 ° C, the liquid component is heated in the distillation apparatus 300, and the substance having a low boiling point, that is, the oil component, first boils to become a gas. The oil component is recovered in a separate container and cooled to obtain a liquid oil, which can be utilized as light oil. As for the constitution of the distillation apparatus 300 for separating the oil component from the separated liquid components as described above, the distillation apparatus 300 of the general constitution in which the respective liquid components are separated by the fractional distillation method is used , And a detailed description thereof will be omitted.

After the non-cohesive oil component is separated from the liquid component of the modified mixture, the liquid component remaining in the distillation apparatus 300 is recovered as an additive (S150). That is, the liquid component remaining in the distillation apparatus 300 without distillation, that is, the dissolved component, can be recovered as an additive after cooling to room temperature. As described above, the modified mixture containing the oil component exists in a liquid state at normal temperature and atmospheric pressure. However, after the oil component having no cohesion is separated from the liquid component of the modified mixture, the modified mixture is present in a solid state . Therefore, the dissolved component remaining in the distillation apparatus 300 after the oil component is separated is solidified upon cooling to room temperature, and is present in a solid state, and can be recovered as an additive added to the coke for producing coke.

Hydrogen donor Additive yield (wt%) G-Factor Remarks Tetralin 50.5 94.39 Conventional technology 1-MN (80%)
+ tetralin (20%) 22.9 96.54 Hydrogenated tar 48.1 96.50 Examples of the present invention

Table 3 is a table for comparing the yield and G-factor of the additives prepared using various hydrogen donors. Referring to Table 3, while tetraline, which has been conventionally used as a hydrogen donor, has a high additive yield with a mass percentage of 50% or more, it has a high yield of additive with a nonhydrogen donating agent such as 1-Methyl Naphthalene (1-MN) When the hydrogen donor, tetralin, was used at a mass percentage of 20%, the additive yield was less than 23%. However, when the additive is prepared using the hydrogen donor according to the present invention, that is, the hydrogenated tar, the additive yield is 48% or more, and it can be understood that the expensive tetralin can be substituted almost 100%.

In addition, in order to examine the effect of the additive prepared using various hydrogen donors on the coke quality, the degree of improvement of the degree of cohesion was evaluated by G-factor analysis. As shown in Table 3, the hydrogen donor The G-factor values are similar to each other. Therefore, the physical properties of the additives prepared using the hydrogenated tar are very similar to those of the additives prepared using tetralin, and therefore, in the production of additives added to the coke for the production of coke, an expensive substitute for tetralin The effect of the additive to be produced can be kept the same even when using hydrogenated tar.

Therefore, according to the method of manufacturing the additive according to the embodiment of the present invention, it is possible to economically substitute the expensive chemical agent used at the time of manufacturing the additive while securing the integrity of the additive, thereby improving the stability of operation according to the process simplification, It is possible to solve the environmental problem caused by the increase in the use of the apparatus.

In addition, the additive can be greatly improved by producing the additive by the method of modifying the unreacted carbon, and the additive can be additionally produced as a by-product.

5 is a block diagram showing a coke making method according to an embodiment of the present invention. Referring to FIG. 5, a method of manufacturing coke according to an embodiment of the present invention includes preparing a coke; Preparing an additive; A process of mixing the coke and the additive; Charging a mixture of coke oven and additive into a coke oven, and carburizing the coke oven to produce a coke. Thereafter, although not separately shown, the process includes extruding the coke produced from the coke oven and digesting the extruded gaseous coke by a wet or nitrogen cooling method.

The process of preparing the coke is a process of preparing the coke to be used for producing the coke, and the process of crushing the coke. Coking coal is a blend of a mixture of coal and may contain strong coals with high cohesiveness, but may contain a large amount of coals with low or no cohesion. This is because the additive according to the embodiment of the present invention can be mixed with the raw coal to impart cohesiveness to the raw coal.

Thus, when the coke is provided, the coke is crushed, and the particle size thereof can be made 10 mm or less. The crushing is performed so that the size of the particle size is 10 mm or less in order to improve the charging density and the fluidity when the coke oven is charged into the coke oven. For example, when the particle size of the crushed coke is more than 10 mm, there is a problem that the gap between the particles becomes large and the charging density is low when they are charged into the coke oven, which may cause the fluidity to deteriorate. Each shredded coking coal is stored in its respective hopper.

When the crushing of each coke is finished, the moisture content is controlled in the drying process by heat-treating the coke, though not shown, at a predetermined temperature. At this time, the content of water contained in each coke can be adjusted to 6 mass% to 10 mass%. The control of the water content is intended to improve the flowability of the raw carbon particles and to increase the charging density by reducing the pores of the raw carbon particles.

As described above, an additive is prepared on the other hand while preparing the raw coal. The process of preparing the additives consists of preparing the additives and crushing the additives. Here, the process of preparing the additive is performed according to the method of manufacturing the additive according to the embodiment of the present invention described above, and a duplicate description will be omitted. When the additive is prepared, the additive in the solid state is crushed, for example, crushed to a particle size of 10 mm or less.

When the crushed coke and the additive are prepared, the prepared coke and additives are mixed in a mixing tank. Here, the compounding tank may be a variety of means capable of mixing the coking coal and the additive, and may be mixed such that the additive is contained in an amount of 1 to 15% by weight in the entire mixture of the coking coal and the additive. For example, when the additive is less than 1 wt%, the effect of improving the strength of the coke due to the improvement of the adhesion due to the additive does not appear, and adding the additive at 15 wt% or more unnecessarily increases the use amount of the additive.

Thereafter, the mixture in which the coke and the additive are mixed is charged into a coke oven, which is then dried to produce coke. For example, when the coke and the additive are mixed, the mixture is charged into a coal bin, and a certain amount of the mixture is charged into the coke oven. At this time, there is also an effect that the charging density and flow rate of the raw coal are increased by the additive. Thereafter, the mixture is dried in a coke oven to produce a high strength coke, and the coke produced is extruded. The extruded coke is extinguished by wet or nitrogen cooling.

Therefore, according to the method of manufacturing coke according to the embodiment of the present invention, high strength coke can be manufactured using coal, especially, a mint point rich in resources and low in cost. Therefore, it is possible to increase the content of unreacted carbon contained in the coking coal, and thus it is possible to economically provide the coke of good quality even when the demand for the coking coal for metallurgy is increased.

While the preferred embodiments of the present invention have been described and illustrated above using specific terms, such terms are used only for the purpose of clarifying the invention, and the embodiments of the present invention and the described terminology are intended to be illustrative, It will be obvious that various changes and modifications can be made without departing from the spirit and scope of the invention. Such modified embodiments should not be individually understood from the spirit and scope of the present invention, but should be regarded as being within the scope of the claims of the present invention.

100: reforming reactor 200: separator
300: distillation device

Claims (13)

As a hydrogen donor used in the preparation of an additive to be added to coke for coke production,
Hydrogen is added to a position where the carbon of the tar formed at the time of carbonization of the coal is connected by a double bond or a triple bond so that the aliphatic carbon and the aromatic carbon contained in the total carbon are contained in a ratio of 1: 0.35 to 1: 0.40 Hydrogen donating agent.
delete The method according to claim 1,
Wherein the hydrogen donor has a boiling point of 200 to 230 DEG C for distilling 10 wt% of the solution, a boiling point of 285 to 300 DEG C for distilling 50 wt% of the solution, and a boiling point of 90 wt% Wherein the temperature is 330 ° C to 360 ° C.
A method for producing an additive added to coke for coke production,
The process of preparing coal;
A process of preparing hydrogenated tar;
Mixing the coal and hydrogenated tar;
Modifying a mixture of coal and hydrogenated tar;
Separating the liquid phase of the modified mixture; And
And recovering the dissolved substance from the liquid phase of the modified mixture,
The process for preparing the hydrogenated tar is performed by adding hydrogen to the tar produced at the time of coal leaching,
Wherein the hydrogenated tar contains aromatic carbon to aliphatic carbon in a ratio of 1: 0.35 to 1: 0.40.
delete delete The method of claim 4,
The boiling point for distilling 10 wt% of the hydrogenated tar is 200 to 230 DEG C, the boiling point for distilling 50 wt% is 285 to 300 DEG C, the boiling point for distilling 90 wt% Lt; RTI ID = 0.0 > 330 C < / RTI >
The method of claim 4,
The process of modifying the mixture of coal and hydrogenated tar,
Reacting the mixture in a reaction vessel having a temperature of 300 ° C to 500 ° C and a pressure of 60 bar to 80 bar for at least 40 minutes.
The method of claim 4,
Before the process of recovering the solute from the liquid phase of the modified mixture,
And separating the non-cohesive oil component from the liquid phase of the modified mixture.
The method of claim 9,
The process of separating the oil component comprises:
Heating the liquid phase of the modified mixture to a temperature above the boiling point of the oil component to separate the oil component from the dissolved component.
The method of claim 9,
The process of separating the oil component comprises:
Heating the liquid phase of the modified mixture to a temperature of 350 ° C to 450 ° C to separate an oil component having a boiling point of less than 350 ° C to 450 ° C from the solution.
The method of claim 4,
Wherein the coal for preparing the additive comprises an untreated carbon.
A method for producing coke by mixing an additive prepared by any one of claims 4 and 12 with coke.

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