KR101726427B1 - Method and apparatus with level senser of suspended catalyst for producing binder for coke - Google Patents

Abstract

A mixing drum for mixing the pretreated coal and the solvent into slurry so that the height of the catalyst layer suspended in the reactor can be detected more quickly and accurately, a reactor for liquefying the coal slurry through the mixing drum, A separator for separating the additive from the liquefied product generated from the reactor, a separator connected between the separator and the mixing drum to separate the oil separated from the separator into a solvent in the mixing drum, There is provided an apparatus for producing an additive for coke comprising a supply line for supplying a catalyst and a detector for detecting the height of a catalyst layer formed by a catalyst suspended in the reactor installed in the reactor, .

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to an apparatus for producing a coke additive having a height detecting device for a suspended catalyst layer in a reactor,

Disclosed is an apparatus and a manufacturing method for a coke additive having a height detecting device for a catalyst layer so that the height of a catalyst layer floating inside a reactor for producing a coke additive can be detected in a non-contact manner.

For example, in the case of a process for producing a quality improving agent to be added for improving the strength of coke or a process for liquefying coal, low-grade raw coal is mixed with a solvent and liquefied under high temperature and high pressure to prepare a coke additive. In the coal liquefaction process, a reaction process of adding hydrogen to the solvent is added to the coal in order to improve the hydrogen transfer capacity.

In this reaction process, a floating catalyst is added to the reactor to increase the coal liquefaction effect or easily attach hydrogen to the solvent. In the circulation process where the solvent and the hydrogen which are not contained in the reactor are included in the upper part of the reactor and the hydrogen and the coal are not supplied, the reaction occurs in which hydrogen or hydrogen is added to the coal or the solvent.

The suspended catalyst used to increase the efficiency of the hydrogenation reaction inside the reactor is not dissolved in the solvent and is floated in the reactor to form the catalyst layer like the reactant pushed from the circulation pump to the solid having a high density.

The top height of the suspended catalyst layer is determined by the amount of reactant pumped by the circulation pump. If the height of the catalyst layer is lower than that of the reactor, the reactant and the hydrogen do not sufficiently react and the hydrogenation efficiency drops. If the height of the catalyst layer is high, the catalyst is transferred to the upper portion of the reactor, thereby promoting wear of the circulation pump and accumulating catalyst at the inlet of the reactor.

Therefore, it is very important to control the height of the catalyst layer suspended in the reactor.

A device for manufacturing a coke additive and a method of manufacturing the additive for coke, which are capable of detecting the height of the catalyst layer suspended in the reactor more quickly and accurately, are provided.

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 COG and / or LNG with cracking gas to the reactor, A separator for separating the additive from the liquefaction product produced from the reactor, a supply line connected between the separator and the mixing drum to supply the oil separated from the separator to the mixing drum as solvent, And a detecting unit for detecting the height of the catalyst layer formed by the suspended catalyst in the reactor.

Wherein the detector is disposed outside the reactor and includes a radiation section for irradiating the radiation for density measurement with the reactor, a detector disposed opposite the radiation section through the reactor for detecting radiation irradiated from the radiation section, A detector for detecting the inner density of the reactor from the signal to calculate the height of the top of the catalyst layer formed by the suspended catalyst suspended inside the reactor; And a moving part for moving the moving part.

The moving unit includes a supporting member for supporting the radiation unit and the detector, a conveying screw that is disposed along the axial direction of the reactor and is coupled to the supporting member to move the supporting member, a driving motor connected to the conveying screw, . ≪ / RTI >

And a guide bar extending from the base plate on which the drive motor is installed and extending along the feed screw and guiding the support member through the support member.

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 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 recycle process in which the liquid phase oil obtained in the separation process is supplied to the coal pretreatment process and used as a solvent, wherein the coal liquefaction process detects the top height of the catalyst layer formed by the suspended catalyst in the reactor for liquefying the coal slurry , And a catalyst layer top height control step.

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

The height detection process may include detecting the internal density of the reactor and calculating the height of the suspended catalyst layer inside the reactor from the internal density of the reactor.

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 performed at a temperature of 250 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 suspended catalyst may include nickel and molybdenum based on alumina Al ₂ O ₃ .

The suspended catalyst may be in the form of a pellet having a particle size of 1.0 to 3.0 mm.

The density of the suspended catalyst may be 0.5 to 0.7 kg / liter.

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.

As described above, according to the present embodiment, the height of the catalyst layer suspended in the reactor can be detected more quickly and accurately, thereby minimizing fluctuations in the flow rate of the circulating pump in the reactor and enhancing the stability of the equipment.

Further, the height of the catalyst layer can be optimized and controlled, and the reaction efficiency can be improved.

Further, the additive for coke can be produced more economically and efficiently.

Fig. 1 is a schematic diagram showing a facility for manufacturing an additive for coke according to this embodiment.
FIG. 2 is a schematic view showing the structure of a catalyst layer height detecting device provided in a reactor of the coke additive manufacturing facility according to the present embodiment.
3 and 4 are schematic views showing the configuration of a moving part of the catalyst layer height detecting device according to the present 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 a constitution of an additive manufacturing facility for coke according to this embodiment.

As shown in FIG. 1, the additive manufacturing apparatus of the present embodiment includes a mixing drum 10 for mixing a pretreated coal with a solvent to make a slurry, a reactor 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) and supplying the oil separated from the separation unit to the mixing drum (10) as a solvent.

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

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 is a vessel which is sufficiently resistant to high temperature and high pressure and has a reaction space therein, and liquefies the coal slurry under high temperature and high pressure.

2, a circulation pump 33 for circulating a reactant is connected to the lower end of the reactor 30, a circulation pump 33 is connected to an upper portion of the reactor 30, And a cup portion 34 for receiving the reacted material transferred to the circulation pump 33. The reactor 30 accommodates a suspended catalyst in order to increase the efficiency of coal liquefaction reaction therein.

For example, the suspended catalyst may include nickel and molybdenum based on alumina Al ₂ O ₃ . The suspended catalyst may be in the form of a pellet having a particle size of 1.0 to 3.0 mm. The density of the suspended catalyst may be 0.5 to 0.7 kg / liter.

The suspended catalyst is suspended in the reactor (30) together with the reactant pushed up by the circulation pump (33) into a solid that is insoluble in the solvent, and forms the catalyst layer (37). The catalyst layer 37 can be understood as a catalyst suspended region formed as the suspended catalyst is floated in the reactor 30. [

Since the amount of the reactant circulating in the reactor 30 is larger than the amount of the solvent to be fed and the reactant must be circulated under high temperature and high pressure, the circulation pump 33 can be a canned type pump.

Accordingly, the coal slurry and the floating catalyst are raised from the lower part to the upper part by the operation of the circulation pump 33 and the liquefaction reaction occurs. The reactant that has reached the cup portion 34 at the upper portion of the reactor 30 flows into the cup portion 34 and flows into the circulation pump 33 through the pipe 35 under the cup portion 34, Recirculated. In the course of the circulation of the reactants, the catalyst layer 37 is formed while the catalyst is floating.

Here, the present embodiment further includes a detection unit 60 for detecting the height of the upper end of the catalyst layer 37 floating inside the reactor 30. [

The height of the catalyst layer 37 in the reactor 30 can be easily checked through the detection unit 60 so that the height of the catalyst layer 37 can be stably controlled and the suspended catalyst can be circulated through the cup portion 34, (33).

2, the detection unit 60 includes a radiation unit 62 disposed outside the reactor 30 to irradiate the radiation to the reactor 30, a radiation unit 62 disposed between the reactor 30 A detector 64 disposed on the opposite side of the catalytic layer 37 to detect the radiation irradiated from the radiation section 62 and a catalyst layer 37 inside the reactor 30 by checking the density inside the reactor from the signal detected by the detector 64, And a controller 60 for controlling the operation of the radiator 62 and the detector 64 to move the radiator 62 and the detector 64 along the axial direction of the reactor 30 to the upper boundary surface position of the catalyst layer, .

The radiation part 62 is sufficient to penetrate the inside of the reactor 30 and detect the density of the suspended material in the reactor 30 irrespective of the thickness of the reactor 30 or the heat ray or the heat insulating material provided on the outer wall of the reactor 30 Any kind of radiation can be applied.

A detector 64 for detecting the radiation irradiated from the radiation section 62 and the radiation section 62 and passing through the reactor 30 is disposed opposite to the reactor 30 via the reactor 30 as shown in FIG. .

The detector 64 detects radiation passing through the reactor 30 and applies an output signal to the arithmetic unit 66.

The calculator 66 can calculate the signal detected by the detector 64 to identify the interface position of the catalyst layer 37 through the difference between the density value in the region where the catalyst exists and the density value in the region without the catalyst. The calculation unit 66 drives the moving unit to move the position of the radiation unit 62 and the detector 64 to a position corresponding to the height of the upper interface plane of the catalyst layer 37. Therefore, the height of the catalyst layer 37 in the reactor 30 can be accurately confirmed through the position of the radiation part 62 and the detector 64.

3 and 4, the moving unit includes a support member 70 for supporting the radiation unit 62 and the detector 64, and a support member 70 disposed side by side along the axial direction of the reactor 30, A driving motor 72 connected to the conveying screw 72 and driven in response to a signal from the arithmetic unit 66 to rotate the sinker screw 72, 74).

The moving unit is provided with a transfer screw 72 on the base plate 76 on which the drive motor 74 is installed so as to more stably move the support member 70 moved up and down along the transfer screw 72 And a guide bar 78 extending through the support member 70 and guiding the support member 70 through the support member 70.

The support member 70 is formed to surround the reactor 30 so as not to interfere with the reactor 30 extending vertically and a radiation unit 62 and a detector 64 are installed at both ends of the support member 70.

A drive motor 74 is installed on a base plate 76 disposed at a lower portion of the reactor 30 and a transfer screw 72 connected to a rotation axis of the drive motor 74 is disposed at a predetermined distance from the reactor 30, 30 in the vertical direction.

The guide plate 78 is provided on both sides of the base plate with the feed screw 72 therebetween. The two guide bars 78 are arranged in parallel with the feed screw 72 and extend in the vertical direction along the reactor 30.

The conveying screw 72 and the guide bar 78 are engaged with the supporting member 70. The conveying screw 72 is screwed to the supporting member 70 and the two guide bars 78 are inserted through the supporting member 70 and the supporting member 70 is slid along the guide bar.

When the driving motor 74 is controlled and operated, the conveying screw 72 is rotated in the forward and reverse directions and the supporting member 70 screwed to the conveying screw 72 is moved up and down along the conveying screw 72. Therefore, the radiation part 62 and the detector 64 installed on the support member 70 move together with the support member 70 and move up and down along the reactor 30.

The driving motor 74 rotates the conveying screw 72 in the forward and reverse directions according to the real time control signal of the calculating section 66 to rotate the supporting member 70 in accordance with the height of the upper surface of the catalyst layer 37, It is possible to position the radiation unit 62 and the detector 64 installed in the apparatus. The height of the catalyst layer 37 is accurately determined by accurately determining the height of the suspended catalyst layer 37 in the reactor 30 through the position of the support member 70 and controlling the drive of the circulation pump 33 of the reactor 30 It becomes possible to control and manage it appropriately.

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.

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 be used as a catalyst. If the amount exceeds the above range, it is difficult to regenerate the catalyst and the catalyst is adversely affected.

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.

A suspension catalyst in the reactor may be used to facilitate the liquefaction reaction. In an embodiment, the floating catalyst may include nickel and molybdenum based on alumina Al ₂ O ₃ . The suspended catalyst may be in the form of a pellet having a particle diameter of 1.0 to 3.0 mm, and the density of the suspended catalyst may be 0.5 to 0.7 kg / liter.

In the present embodiment, the coal liquefaction process may include a height detecting step of detecting the height of the upper end of the catalyst layer floating in the reactor for liquefying the coal slurry, and a height control step of controlling the height of the catalyst layer.

The height detection process may include detecting the internal density of the reactor, and calculating the height of the catalyst layer suspended in the reactor from the internal density of the reactor.

The height of the catalyst layer in the reactor is detected by irradiating the outside of the reactor with radiation. The detector detects the radiation passing through the reactor and applies the output signal to the operation unit. The calculation unit calculates the density inside the reactor from the output signal of the detector and calculates the position of the upper boundary surface of the catalyst layer through the density difference between the region having the floating catalyst and the region having no floating catalyst.

For example, the density of the region where the solvent and the gas and the suspended catalyst are mixed is approximately 0.72 to 0.96 g / cm 3, the density of the solvent and gas only mixed region without catalyst is approximately 0.4 to 0.7 g / cm 3, The area where the catalyst is present can be identified.

By detecting the boundary position between the regions where the density is changed through the irradiation of the radiation, the height of the top of the catalyst layer can be accurately confirmed.

The height of the catalyst layer floating inside the reactor can be precisely checked from the outside so that the circulation pump at the bottom of the reactor is finally controlled to control the height of the catalyst layer appropriately.

In this embodiment, the coal liquefaction process can be carried out at a temperature of 250 to 450 DEG C and a pressure of 30 to 120 bar. The pressure inside the reactor can be controlled by adjusting the supply flow rate of the cracking gas.

As the inside of the reactor is set to the above temperature and pressure range, 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 250 ° 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 is hardened and hardened.

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 step, 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 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 250 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
33: circulation pump 34:
35: pipe 37: catalyst layer
40: separator 42: separator
44: Filter device 46: Distiller
50: supply line 60:
62: radiation part 64: detector
66: computing unit 70: supporting member
72: Feed screw 74: Drive motor
78: Guide Bar

Claims (17)

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 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 height detection step of detecting a top height of a catalyst layer formed by a floating catalyst suspended in a reactor for liquefying a coal slurry, and a catalyst layer top height control step,
Wherein the height detecting step includes a step of detecting the internal density of the reactor and a step of calculating the height of the catalyst layer suspended in the reactor from the internal density of the reactor, . The method according to claim 1,
A method for producing an additive for coke, comprising the step of introducing a dispersed iron catalyst into the reactor during the pretreatment of coal. 3. The method of claim 2,
Wherein the dispersed iron catalyst is Fe ₂ O ₃ . The method of claim 3,
Wherein the dispersed iron catalyst is charged in an amount of 0.5 to 3.0 parts by weight based on 100 parts by weight of coal. delete The method according to claim 1,
Wherein the coal liquefaction process is performed at a temperature of 250 to 450 DEG C and a pressure of 30 to 120 bar. The method according to claim 6,
Wherein the coal liquefying process comprises heating the cracking gas at 400 to 600 ° C to supply the catalyst to the reactor. The method according to claim 1,
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 supplying the oil separated from the additive in the fractional distillation step to the coal pretreatment step. 9. The method of claim 8,
Wherein the filtration step is performed at a temperature of 120 to 400 ° C. 10. The method of claim 9,
Wherein the fractionation step is performed at a temperature of 350 to 450 ° C. A mixing drum for mixing the pretreated coal with a solvent to form a slurry, a reactor for liquefying the coal slurry through the mixing drum, a gas supply unit for supplying COG and / or LNG with the cracking gas to the reactor, A supply line connected between the separation unit and the mixing drum to supply the oil separated from the separation unit to the mixing drum as a solvent, and a supply line provided in the reactor, And a detecting section for detecting the height of the formed catalyst layer,
Wherein the detector is disposed outside the reactor and comprises a radiation section for irradiating the radiation for density measurement with the reactor, a detector disposed opposite the radiation section through the reactor for detecting radiation irradiated from the radiation section, And a control unit for controlling the radiation unit and the detector according to the control signal of the calculation unit to the upper height of the catalyst layer along the axial direction of the reactor And a moving part for moving the catalyst in the catalyst-containing catalyst layer. 12. The method of claim 11,
And a catalyst supply unit for supplying the dispersion catalyst to the mixing drum. The apparatus for producing an additive for coke according to claim 1, 13. The method of claim 12,
Wherein the catalyst supply unit is provided with a dispersion type iron catalyst. 12. The method of claim 11,
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 distillation unit connected to the mixing drum through an inlet of the mixing drum to supply the oil separated from the additive to the mixing drum. delete 12. The method of claim 11,
The moving unit includes a supporting member for supporting the radiation unit and the detector, a conveying screw that is disposed along the axial direction of the reactor and is coupled to the supporting member to move the supporting member, An apparatus for manufacturing an additive for coke comprising a height detecting device for a suspended catalyst layer inside a reactor including a motor. 17. The method of claim 16,
Further comprising a guide bar extending from the base plate on the base plate on which the drive motor is installed, the guide bar penetrating the support member and guiding the support member.

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