KR101751522B1 - Method and apparatus for producing binder for coke - Google Patents

Abstract

A coal pretreatment step which is optimized for extracting additive for coke and which slurries coal by dispersing it in a solvent so that additives can be easily and effectively produced; A coal liquefaction process for liquefying coal slurry by reacting coal slurry with cracking gas; A step of supplying COG and / or LNG with a cracking gas during a coal liquefaction process; A separation step of separating the additive from the liquefied product; And a recycling step of supplying the liquid oil obtained in the separation step to the coal pretreatment step and using the oil as a solvent, wherein the coal liquefaction process comprises a first step of softening the coal slurry through the first reactor, And a second step of substantially cracking the coal slurry via the second reactor.

Description

TECHNICAL FIELD [0001] The present invention relates to an additive for coke,

A manufacturing method and an apparatus for manufacturing an additive for coke used for improving coke strength are disclosed.

Generally, coke is produced through a coke making process using coking coal. The coking coal used to manufacture the coke is classified as hard-boiled and un-boiled, depending on the degree of cohesion. For stable operation of large blast furnaces, the use of high-strength coke is required. In order to produce a high-strength coke, it is advantageous to use strong coals having excellent cohesiveness or to use a large amount of coals compared to uncoated coals. In the meantime, a large amount of high-priced, high-priced strong coals has been used 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. Accordingly, the development of a technique for manufacturing high-strength coke while using low-cost and low-cost coking coal such as bituminous coal or lignite as coking coal is actively under way.

For example, a technique has been developed for producing a quality improving agent for coke production through a sales method in which a low-grade raw material is dissolved in an expensive supercritical solvent under a high-temperature and high-pressure condition to extract a cohesive substance.

However, nowadays, the focus is mainly on the production of oil from coal, so there is no optimized process for the extraction of additives, which is insufficient to produce additives effectively. In addition, there is a problem that the economical efficiency in production of additives is inferior due to frequent breakdown and new operating know-how by using existing coal direct liquefaction type process.

A method and an apparatus for manufacturing an additive for coke which are optimized for extracting additive for coke.

The present invention also provides a method and an apparatus for manufacturing an additive for coke which is capable of easily and effectively producing an additive for improving coke strength through a coal liquefaction process optimized for additive extraction.

Further, there is provided a method and an apparatus for manufacturing an additive for coke which is capable of producing an additive without constructing a large-scale facility such as a hydrogenation plant.

Further, a method and an apparatus for manufacturing additive for coke that can simplify the manufacturing process are provided.

The present invention also provides a method of manufacturing an additive for coke and an apparatus for producing the additive for coke using low-grade carbon.

The additive manufacturing method of this embodiment includes: a coal pretreatment step of dispersing coal into a slurry by dispersing it in a solvent; A coal liquefaction process for liquefying coal slurry by reacting coal slurry with cracking gas; A step of supplying COG and / or LNG with a cracking gas during a coal liquefaction process; A separation step of separating the additive from the liquefied product; And a recycling step of supplying the liquid oil obtained in the separation step to the coal pretreatment step and using the oil as a solvent, wherein the coal liquefaction process comprises a first step of softening the coal slurry through the first reactor, And a second step of substantially cracking the coal slurry via the second reactor.

In the coal liquefaction process, a fluidized bed reactor may be used as the first reactor and a slurry reactor may be used as the second reactor, and the coal slurry may be subjected to the first process and the second process sequentially through the fluidized bed reactor and the slurry reactor.

In the coal liquefaction process, a fluidized bed reactor may be used as the first reactor and the second reactor, and the first and second processes may be performed while the coal slurry is sequentially passed through the plurality of fluidized bed reactors.

In the coal liquefaction process, a slurry reactor may be used as the first reactor and the second reactor, and the first and second processes may be performed while the coal slurry is sequentially passed through the plurality of slurry reactors.

The method may further include a step of adding a dispersed iron catalyst when the coal pretreatment process is performed.

The coal pretreatment step may further include pulverizing coal and drying the pulverized coal.

The coal may comprise lignite or sub-bituminous coal.

In the coal pulverization step, the coal may be pulverized to a size of 60 mesh or less.

The step of drying the coal may include drying the coal so that the moisture content of the coal is 10 wt% or less.

The coal pretreatment may be performed by mixing the dried coal with the solvent at a weight ratio of 1/1 to 1/4 to form a slurry.

The dispersed iron catalyst may be Fe ₂ O ₃ .

The dispersed iron catalyst may be added in an amount of 0.5 to 3.0 parts by weight based on 100 parts by weight of coal.

The coal liquefaction process may be carried out at a temperature of 350 to 450 DEG C and a pressure of 30 to 120 bar.

The coal liquefaction process may be performed by heating the cracking gas at 400 to 600 ° C.

The separation step includes a separating step of separating the gas component from the liquefied product, a filtration step of separating the liquid material and the solid matter, and a fractionation step of distilling the liquid material separated in the filtration step to separate the additive And the recycle process may be such that the oil separated from the additive in the fractional distillation step is supplied to the coal pretreatment process.

The filtration step may be performed at a temperature of 120 to 400 ° C.

The fractionation step may be carried out at a temperature of from 350 to 450 < 0 > C.

The manufacturing apparatus of this embodiment includes a mixing drum for mixing a pretreated coal and a solvent into a slurry, a reactor for liquefying the coal slurry through the mixing drum, a gas supply unit for supplying a cracking gas to the reactor, a liquefied product And a supply line connected between the separating unit and the mixing drum to supply the oil separated in the separating unit to the mixing drum as a solvent, wherein the reactor softens the coal slurry primarily And a second reactor connected to a downstream end of the first reactor to substantially crack the coal slurry passing through the first reactor.

The first reactor may be a fluidized bed reactor and the second reactor may be a slurry reactor.

The first reactor and the second reactor may be fluidized bed reactors.

The first reactor and the second reactor may be slurry reactors.

The production apparatus may further include a catalyst supply unit for supplying the dispersion catalyst to the mixing drum.

The separator includes a separator for separating the gas component from the liquefaction process product, a filter device connected to the separator for separating the liquid material and the solid material, and a separator for separating the additive from the liquid material, And a distiller which is connected to the mixing drum through a pipe and supplies the oil separated from the additive to the mixing drum.

The manufacturing apparatus may further include a crusher for crushing coal for pretreatment of coal, and a drier for drying the crushed coal.

The catalyst supply unit may be a structure for supplying a dispersed iron catalyst.

The gas supply unit may be a structure for supplying COG and / or LNG.

As described above, according to this embodiment, an optimized additive manufacturing process can be realized.

In addition, it is possible to produce additives for coke more economically and efficiently by optimizing an additive manufacturing process.

In addition, it is possible to maximize the productivity of the additive by increasing the reactivity in the reactor.

1 is a schematic structural view showing an apparatus for producing additive for coke according to this embodiment.
FIG. 2 is a view showing the reactor construction more specifically of the apparatus for producing additive for coke according to the present embodiment.
3 and 4 are views showing reactor configurations according to another embodiment.

The terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the invention. The singular forms as used herein include plural forms as long as the phrases do not expressly express the opposite meaning thereto. Means that a particular feature, region, integer, step, operation, element and / or component is specified, and that other specific features, regions, integers, steps, operations, elements, components, and / And the like.

Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings so that those skilled in the art can easily carry out the present invention. It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit or scope of the invention. Accordingly, the present invention may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.

Fig. 1 schematically shows the construction of an apparatus for producing additive for coke according to this embodiment.

1, the manufacturing apparatus of the present embodiment includes a mixing drum 10 for mixing a pretreated coal and a solvent into a slurry, a reactor 30 for liquefying coal slurry through the mixing drum 10 A separator 40 for separating the additive from the liquefied product generated from the reactor 30 and a separator 40 for separating the additive from the liquefied product generated from the reactor 30, And a supply line (50) connected between the mixing drum (10) to supply the oil separated in the separation part to the mixing drum (10) as a solvent.

The production apparatus may further include a catalyst supply unit 20 for supplying the dispersion catalyst to the mixing drum 10.

In addition, the manufacturing apparatus may further include a crusher 12 for crushing coal and a drier 14 for drying the crushed coal to pretreat coal.

In this embodiment, the raw material for the additive manufacturing coal may include low-grade non-coking coal such as lignite and sub-bituminous coal. Low-grade carbon such as lignite and bituminous coal has low physical properties such as cohesiveness, but it is rich in resources and low in cost, so that it is possible to lower the production cost when manufacturing additive for coke.

The mixing drum 10 mixes the pretreated coal with a solvent to form a coal slurry.

In this embodiment, the solvent introduced into the mixing drum 10 is structured such that the additive is finally separated through the separator 40 and the remaining oil is utilized.

To this end, the supply line 50 is connected between the separating section 40 and the mixing drum 10 so that the oil remaining after the additive separation is supplied via the supply line 50 to the mixing drum 10 as solvent and recirculated .

As described above, the liquid oil separated through the separating unit 40 is directly supplied to the mixing drum 10 and recycled as a solvent, so that the equipment can be simplified, and the process can be simplified to reduce the cost of producing the additive.

The catalyst supply unit 20 is connected to the mixing drum 10 to supply a dispersed iron catalyst. Thus, the dispersed iron catalyst is uniformly mixed with the coal and the solvent in the mixing drum 10.

In this embodiment, the dispersed iron catalyst may be Fe ₂ O ₃ . By adding the dispersed iron catalyst to the coal slurry in this way, the reactivity in the liquefaction reaction can be increased. Accordingly, even when COG or LNG is used as the cracking gas in the liquefaction reaction, the dispersed iron catalyst can increase the reactivity and can obtain a sufficient reaction effect for the production of the additive.

The mixed coal slurry in the mixing drum 10 is conveyed to the reactor 30 by a high-pressure pump. The amount of heat is supplied to the coal slurry through the heating unit 16 provided between the mixing drum 10 and the reactor 30 in the process of transferring the coal slurry from the mixing drum 10 to the reactor 30, .

The reactor (30) liquefies the coal slurry under high temperature and high pressure.

In this embodiment, as shown in FIG. 2, the reactor 30 is structured such that two of the reactors 30 are sequentially connected to one another along the moving direction of the coal slurry in the process. For convenience of the following description, the reactor disposed in front of the process is referred to as a first reactor 34, the reactor continuously disposed after the first reactor is referred to as a second reactor 36, Quot; reactor "

As shown in FIG. 2, the reactor 30 may be configured such that the first reactor 34 comprises a fluidized bed reactor and the second reactor 36 comprises a slurry reactor. Fluidized bed reactors refer to EBR (Ebullated Bed Reactor) or FBR (Fluidized Bed Reactor) reactors. The fluidized bed reactor is provided with a drive pump for recycling the coal slurry in the reactor to the bottom. As the coal slurry flows into the fluidized bed reactor, it becomes thermally softened and cracking occurs gradually and it is liquefied. At this time, the recycle drive pump installed at the lower part is operated to recycle the coal slurry therein in a large amount relative to the inflow amount. By doing so, homogenization of components in the reactor and temperature gradient from the inlet to the outlet can be maintained at 5 ° C or less. Since many techniques are disclosed for a fluidized bed reactor, a detailed description of its structure is omitted.

The slurry reactor is a Slurry Bubble Column Reactor (SBCR) or a Slurry Phase Reactor (SPR) reactor, and means a reactor for forming a slurry of a gas bubble in a liquid. The coal slurry is introduced into the slurry reactor and thermally softened, and the cracks are progressively cracked as they rise to the upper part and are liquefied. The slurry reactor is simple in structure and has a sufficient height so that the reaction occurs while the coal slurry rises from the bottom to the top. Since the slurry reactor also has many techniques for its structure, detailed description is omitted.

As described above, in this embodiment, the coal slurry is primarily liquefied through the slurry reactor, which is the second reactor 36 after passing through the fluidized bed reactor, which is the first reactor 34, thereby maximizing the cracking efficiency.

The first reactor 34 receives the mixed coal slurry from the mixing drum and thermally processes the coal slurry for a sufficient time to increase the reactivity. If the fluidized bed reactor is used in the first reactor 34, the softening process proceeds while recycling the coal slurry for a sufficient period of time to facilitate liquefaction of the coal slurry.

The second reactor 36 is discharged from the first reactor 34 to substantially crack the supplied coal slurry. Substantially means that cracking is mainly performed in the second reactor 36 relatively to the first reactor 34. [ When a slurry reactor is used in the second reactor 36, hydrocarbons can be directly discharged from the upper portion after cracking because only a rising stream exists in the reactor. Therefore, it is possible to prevent the hydrocarbons decomposed by the cracking from returning to the coal, which is a polymer structure. In the conventional case, the coal slurry resides in the reactor for a long time while the hydrocarbon decomposed by the cracking returns to the coal.

As described above, the reactor of the present embodiment liquefies the coal slurry sequentially through the first reactor 34 and the second reactor 36, thereby improving the process efficiency.

3 and 4, in the reactor of this embodiment, the first reactor and the second reactor are both formed of a fluidized bed reactor, or both the first reactor and the second reactor may be a slurry reactor .

The gas supply unit 32 is connected to one side of the reactor 30 to supply a cracking gas to the reactor 30. In the present embodiment, the gas supply unit 32 supplies COG (Coke Oven Gas), LNG (Liquefied Natural Gas), or a combination thereof as a cracking gas.

Thus, by using COG or LNG as the cracking gas, the apparatus of this embodiment does not need to be provided with a conventional hydrogen production facility. The hydrogen production facility is very complicated as it is known. The construction cost is 1/4 of the total installation cost and the operation cost is also high. Therefore, in the case of this embodiment, since it is not necessary to construct a hydrogen production facility, the entire plant scale can be reduced and the production cost of the additive can be greatly reduced.

The separation unit 40 includes a separator 42 for separating the gas component from the liquefied product, a filter device 44 connected to the separator for separating the liquid material and the solid material, And a distiller 46 for separating the coke additive (B) by distillation.

The distiller 46 of the separator 40 is connected to the mixing drum 10 via a supply line 50. Thus, the oil separated from the additive via the still 46 is supplied to the mixing drum 10 through the supply line. The distiller (46) may be a fractionator which separates the additive using the difference in boiling point.

Thus, the apparatus can finally produce the coke additive (B) through the separator (40).

Hereinafter, an additive manufacturing process according to this embodiment will be described.

Hereinafter, the present embodiment will be described by taking as an example the process of manufacturing the additive from the embodiment of Figs. 1 and 2. Fig.

The process for preparing the additive includes a coal pretreatment process in which coal is slurried and dispersed in a solvent, a coal liquefaction process in which a coal slurry is reacted with a cracking gas to liquefy a coal slurry, a COG and / or LNG as a cracking gas in a coal liquefaction process A separating step of separating the additive from the liquefied product, and a recycling step of supplying the liquid oil obtained in the separating step to the coal pretreatment step and using it as a solvent.

In addition, the manufacturing process of the present embodiment may further include a step of charging the dispersed iron catalyst during the coal pretreatment.

The coal pretreatment process is a process of preparing coal as a raw material for the preparation of additives by pulverizing the coal and then drying the pulverized coal.

Coal as raw material is low tin (or low grade) coal with low or no cohesion and low price, and lignite, bituminous coal can be used. Low-grade coal such as lignite and bituminous coal is crushed through a crusher. The pulverization of the coal can be carried out, for example, to a size of 60 meshes or less.

The pulverized coal is subjected to a drying process to remove moisture. Moisture of coal interferes with the mixing of coal and solvent and makes reactor pressure unstable, which lowers reaction efficiency. In this embodiment, the coal is dried so as to have a water content of 10 wt% or less through the coal drying process. When the water content of the coal exceeds 10 wt%, the process efficiency is lowered and additional waste gas treatment steps are required.

The pulverized and dried coal is mixed with a solvent and slurried. In this embodiment, the coal dried for the solvent is mixed at a weight ratio of 1/1 to 1/4.

When the ratio of coal to the solvent is larger than 1/1, the amount of the solvent is small and the coal slurry is not well formed. Thus, the conversion rate of coal in the reactor is also lowered. When the ratio of coal to solvent is lower than 1/4, the viscosity of the coal slurry is lowered by adding too much solvent, and the throughput is increased in each step, thereby increasing the scale of the equipment. As a result, equipment costs and utility usage are increased, resulting in cost problems.

Here, the solvent may be an oil remaining after the additive is finally separated through an additive manufacturing process.

The dispersed iron catalyst may be added during the coal pretreatment.

In this embodiment, the dispersed iron catalyst may be Fe ₂ O ₃ . As described above, by adding the dispersed iron catalyst and mixing it with the coal slurry, the reactivity in the liquefaction reaction can be increased.

The dispersed iron catalyst may be added in an amount of 0.5 to 3.0 parts by weight based on 100 parts by weight of coal.

When the amount of the dispersed iron catalyst is less than the above range, the catalyst can not act as a catalyst. If the amount exceeds the above range, it is difficult to regenerate the catalyst and the catalyst is too much.

The coal slurried through the above process is transferred to the reactor and subjected to a coal liquefaction process. The coal slurry is heated to the desired temperature through the heating process during the transfer to the liquefaction process.

The coal liquefaction process is a process of liquefying the coal slurried at a sufficiently high temperature in the pretreatment process. The coal slurry and the cracking gas are introduced into the reactor and the liquefaction reaction is carried out under the set temperature and pressure.

In this embodiment, the coal liquefaction process includes a first process for softening the coal slurry via the first reactor and a second process for substantially cracking the coal slurry through the second reactor in succession to the first process.

In the coal liquefaction process, the coal slurry is liquefied by sequentially passing through the fluidized bed reactor, which is the first reactor, and the slurry reactor, which is the second reactor.

In the case of the structure shown in FIG. 3, in the coal liquefaction process, the first slurry and the second slurry are sequentially passed through the two fluidized bed reactors, and in the case of the structure shown in FIG. 4, The first process and the second process can be performed while sequentially passing through the process.

In this embodiment, the coal liquefaction process can be performed at a temperature of 350 to 450 DEG C and a pressure of 30 to 120 bar. The pressure inside each reactor can be controlled by adjusting the supply flow rate of the cracking gas.

As the inside of each reactor is formed in the temperature and pressure ranges, a liquefaction reaction proceeds in a mixture of coal and a solvent, that is, a coal slurry. At this time, the supplied cracking gas not only regulates the pressure inside the reactor, but also serves to liquefy the broken loop between the carbon atoms constituting the coal.

When the temperature is lower than 350 ° C in the coal liquefaction process, the coal is not melted and the liquefaction process does not proceed. When the temperature exceeds 450 ° C, the coal is caulked and the coal hardens and the reaction is lowered.

Also, when the reaction pressure is less than 30 bar in the liquefaction process of coal, the pressure in the reactor is low so that donation of hydrogen to coal does not occur. If the pressure exceeds 120 bar, hydrogen will be excessively supplied to the coal, resulting in a reduction in the final production of coke additive, and an increase in the production of undesirable materials such as oil.

In the coal liquefaction process, COG, LNG, or a mixed gas thereof may be supplied as the cracking gas.

Depending on the process conditions, either COG or LNG can be selectively used in the reactor, or both COG and LNG can be used to feed the reactor.

Thus, by using COG or LNG, the production amount of liquefied oil is reduced and the amount of additive produced is increased in the coal liquefaction process.

The cracking gas may be supplied by heating at 400 to 600 ° C in accordance with the internal temperature of the reactor in which the coal liquefaction reaction is performed. Therefore, when the cracking gas is introduced, the change in the temperature inside the reactor is minimized, and the degradation of reactivity can be prevented.

The coal slurry undergoes a thermal process so as to be more easily liquefied through the first process. That is, the coal slurry is softened and liquefied through sufficient time and circulation in the first reactor. The coal slurry after the first step is substantially cracked through the second step. The coal slurry supplied to the second reactor is cracked by the internal upward flow, and then the hydrocarbon is directly discharged to the upper part.

As described above, in this embodiment, the liquefaction process is divided into the first process and the second process and proceeds sequentially, whereby the efficiency of liquefying coal slurry can be further improved.

The product produced in the coal liquefaction process can be separated into coke additive, which is the final target through the separation process.

In this embodiment, the separation step is a step of separating the gas components sequentially from the liquefaction process product, a filtration step of separating the liquid material and the solid matter, and a step of distilling the liquid material separated in the filtration step, And a fractional distillation step of separating the mixture.

The products liquefied through the coal liquefaction process include both solid products, liquid products and gaseous products. The liquid product includes an additive for coke and an oil, and the gaseous product may include fuel gas, sulfur, ammonia, and the like.

The separation step is to separate from the rating of the light gas component (C1 to _{C5, H 2 S, NH 3} , H 2 , etc.) the product of the substance produced through the coal liquefaction process. In the filtration step, the product is separated into a solid product and a liquid product.

The fractionation step following the filtration step is to distill off the liquid product separated in the filtration step, finally obtaining the coke additive separately.

In this embodiment, the filtration step may be performed at a temperature of 120 to 400 ° C.

The coke additive has a softening point of about 120 캜. Therefore, when the temperature is lower than 120 캜 in the filtration step, the additive for coke is present as a solid product, and since the solid product and the additive for coke are mixed, only the additive for coke can not be separated. The filtration step is performed at a temperature of 120 ° C or higher in consideration of the softening point of the additive for coke.

Also, as mentioned above, since the coal liquefaction process is performed at a temperature of 350 to 450 ° C., the initial product produced in the coal liquefaction process is present at a high temperature of 120 to 400 ° C., unless it is cooled. Therefore, when the filtration step is performed immediately after the coal liquefaction process without further heating the product in the filtration step, the filtration process can be performed at a temperature of 120 ° C or higher using the heat of the product. Therefore, in this embodiment, it is necessary to perform the filtration step immediately before the temperature of the product is lowered below 120 캜 immediately after the coal liquefaction process.

In the fractional distillation step, the liquid product separated through the filtration step is distilled using a distiller to obtain an additive for coke.

As mentioned above, the liquid product separated in the filtration step contains oil as well as additives for coke, and it may further include some fuel gas, sulfur, ammonia and the like depending on the temperature.

Fractional distillation which is usually used in the above fractionation stage can be used.

In this embodiment, the fractional distillation step may be carried out at a temperature of from 350 to 450 < 0 > C. Since the oil of the liquid product has a boiling point lower than 350 to 450 ° C, the oil is separated and removed from the liquid product by fractional distillation to obtain an additive for coke. That is, when the liquid product is heated at a temperature of 350 ° C to 450 ° C in the fractional distillation step, the oil is evaporated and only the additive for coke can be separated from the residue. The oil is then separated through a fractional distillation step to finally obtain an additive for coke.

The recycle process recycles the oil obtained in the separation process to the coal pretreatment process so that the oil is used as a solvent in the coal slurry process.

In this embodiment, the recycle process is to feed the oil obtained through the fractional distillation step directly to the mixing drum of the coal pretreatment process. Thus, the oil separated in the separation step can be recycled directly to the coal pretreatment process, thereby simplifying the process.

While the present invention has been described in connection with what is presently considered to be practical exemplary embodiments, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, Of course.

10: mixing drum 12: crusher
14: dryer 20: catalyst supplier
30: Reactor 32: Gas supply part
34: first reactor 36: second reactor
40: separator 42: separator
44: Filter device 46: Distiller
50: supply line

Claims (20)

A coal pretreatment step of dispersing coal into a slurry by dispersing it in a solvent;
A coal liquefaction process for liquefying coal slurry by reacting coal slurry with cracking gas;
A step of supplying COG and / or LNG with a cracking gas during a coal liquefaction process;
A separation step of separating the additive from the liquefied product; And
And a recycle process in which the liquid oil obtained in the separation process is supplied to the coal pretreatment process and used as a solvent,
The coal liquefaction process includes a first step of softening the coal slurry through the first reactor and a second step of continuously cracking the coal slurry through the second reactor in the first step, ≪ / RTI >
Further comprising the step of adding a dispersed iron catalyst during the pretreatment of coal,
The separation step includes a separating step of separating the gas component from the liquefied product, a filtration step of separating the liquid material and the solid matter, and a fractionation step of distilling the liquid material separated in the filtration step to separate the additive and,
Wherein the recycle step comprises feeding the oil separated from the additive in the fractional distillation step to the coal pretreatment step. The method according to claim 1,
Wherein the coal liquefying process uses a fluidized bed reactor as the first reactor and a slurry reactor as the second reactor so that the coal slurry is sequentially passed through the fluidized bed reactor and the slurry reactor to perform the first and second processes. The method according to claim 1,
Wherein the coal liquefaction process uses a fluidized bed reactor as a first reactor and a second reactor, wherein the first and second processes are performed while the coal slurry is sequentially passed through the plurality of fluidized bed reactors. The method according to claim 1,
Wherein the coal liquefaction process uses a slurry reactor as a first reactor and a second reactor, wherein the coal slurry is sequentially passed through a plurality of slurry reactors to perform a first process and a second process. delete The method according to claim 1,
Wherein the dispersed iron catalyst is Fe ₂ O ₃ . The method according to claim 6,
Wherein the dispersed iron catalyst is added in an amount of 0.5 to 3.0 parts by weight based on 100 parts by weight of coal. The method according to claim 1,
Wherein the coal liquefaction process is performed at a temperature of 350 to 450 DEG C and a pressure of 30 to 120 bar. 9. The method of claim 8,
Wherein the coal liquefaction process is performed by heating the cracking gas at 400 to 600 ° C. delete The method according to claim 1,
Wherein the filtration step is performed at a temperature of 120 to 400 ° C. 12. The method of claim 11,
Wherein the fractionation step is carried out at a temperature of from 350 to < RTI ID = 0.0 > 450 C. < / RTI > A mixing drum for mixing the pretreated coal and the solvent to form a slurry,
A reactor for liquefying the coal slurry passed through the mixing drum,
A gas supply unit for supplying COG and / or LNG as a cracking gas to the reactor,
A separator for separating the additive from the liquefaction product produced from the reactor, and
And a supply line connected between the separation unit and the mixing drum to supply the oil separated in the separation unit to the mixing drum as a solvent,
The reactor includes a first reactor for firstly softening the coal slurry and a second reactor for cracking the coal slurry passing through the first reactor connected to the downstream end of the first reactor and relatively mainly cracking compared to the first reactor In addition,
Further comprising a catalyst supplier for supplying the dispersed iron catalyst to the mixing drum,
The separator includes a separator for separating the gas component from the liquefaction process product, a filter device connected to the separator for separating the liquid material and the solid material, and a separator for separating the additive from the liquid material, And a distiller connected to the mixing drum through the inlet of the mixing drum to supply the oil separated from the additive to the mixing drum. 14. The method of claim 13,
Wherein the first reactor is a fluidized bed reactor and the second reactor is a slurry reactor. 14. The method of claim 13,
Wherein the first reactor and the second reactor are fluidized bed reactors. 14. The method of claim 13,
Wherein the first reactor and the second reactor are slurry reactors. delete delete delete delete

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