KR20170074046A - Apparatus for producing binder for coke - Google Patents

Abstract

A mixer for mixing a pre-treated coal and a solvent to make a slurry so that the slurry can be mixed more effectively in manufacturing the additive for coke, a catalyst supplier for supplying the dispersed iron catalyst to the mixer, A gas supply unit for supplying COG and / or LNG as cracking gas to the reactor, a separator for separating the additive from the liquefied product produced from the reactor, a separator for separating the additive from the liquefied product generated from the reactor, And a supply line for supplying the oil to the mixer as a solvent.

Description

[0001] APPARATUS FOR PRODUCING BINDER FOR COKE [0002]

Disclosed is a production apparatus for producing an additive for coke used for improving coke strength.

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.

Accordingly, it is required to develop an optimized and differentiated technique capable of effectively producing additive for coke.

Provided is an apparatus for manufacturing an additive for coke which is capable of mixing a slurry more effectively in the production of an additive for coke.

The present invention also provides an apparatus for manufacturing an additive for coke, which can prevent the slurry from sticking to the inner surface of the mixer during mixing of the slurry.

The manufacturing apparatus of this embodiment includes a mixer for mixing a pretreated coal and a solvent into a slurry, a catalyst supply unit for supplying the dispersed iron catalyst to the mixer, a reactor for liquefying the coal slurry through the mixer, A separator for separating the additive from the liquefied product generated from the reactor, and a separator connected between the separator and the mixer to supply the oil separated from the separator to the mixer as a solvent, wherein the COG and / And a supply line.

Wherein the mixer includes a mixing tank in which coal and a solvent are mixed and mixed, a rotation shaft rotatably installed in the center of the mixing tank, at least one stirring blade installed on the rotation shaft at intervals along the axial direction, And a driving unit for driving the driving unit.

The mixer may further include a circulation pipe through which the slurry is circulated by connecting a bottom portion and an upper portion of the mixing tank, and a circulation pump installed at one side of the circulation pipe and circulating and stirring the slurry in the mixing tank.

The mixer may further include at least one baffle provided at an interval on the inner circumferential surface of the mixing tank and protruding toward the center portion.

The baffle may extend from the top to the bottom along the axial direction of the mixing tank.

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 an oil separator connected to the mixer through the oil separator and supplying the oil separated from the additive to the mixer.

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

The coal may comprise lignite or sub-bituminous coal.

The pulverizer can pulverize coal to a size of 60 mesh or less.

The dryer may be configured to dry the coal so that the moisture content of the coal is 10 wt% or less.

The catalyst supply unit may be configured to supply Fe ₂ O ₃ as a dispersed iron catalyst.

The catalyst supply unit may be charged with 0.5 to 3.0 parts by weight of the dispersed iron catalyst per 100 parts by weight of coal.

As described above, according to this embodiment, the slurry can be mixed more effectively, thereby reducing the time required for mixing the slurry and increasing the production amount of the additive for coke.

In addition, the temperature inside the tank can be homogenized when the slurry is mixed, and the slurry is prevented from sticking to the inner surface of the tank, thereby making it possible to produce the additive for coke more economically and efficiently.

1 is a schematic structural view showing an apparatus for producing additive for coke according to this embodiment.
2 is a schematic cross-sectional view showing a mixer of an apparatus for producing additive for coke according to this 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.

As shown in FIG. 1, the additive manufacturing apparatus of the present embodiment includes a mixer 10 for mixing a pretreated coal and a solvent into a slurry, a catalyst supply unit 20 for supplying a dispersion catalyst to the mixer 10, A reactor 30 for liquefying a coal slurry through the reactor 10, a gas supply 32 for supplying a cracking gas to the reactor 30, a separator 30 for separating the additive from the liquefied product generated from the reactor 30, And a supply line 50 connected between the separator 40 and the mixer 10 to supply the oil separated from the separator to the mixer 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 mixer 10 mixes the pretreated coal with a solvent to form a coal slurry.

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

To this end, the feed line 50 is connected between the separator 40 and the mixer 10 so that the oil remaining after the additive separation is recycled as solvent to the mixer 10 via the feed line 50.

As described above, the liquid oil separated through the separator 40 is directly supplied to the mixer 10 and recycled as a solvent, so that the facility 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 mixer 10 to supply a dispersed iron catalyst. Thus, the dispersed iron catalyst is evenly mixed with the coal and the solvent in the mixer 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 mixer 10 is conveyed to the reactor 30 by a high-pressure pump. The coal slurry is supplied to the coal slurry through the heating unit 16 provided between the mixer 10 and the reactor 30 in the process of transferring the coal slurry from the mixer 10 to the reactor 30, can do.

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.

A heater or the like for applying thermal energy to the reactor 30 is installed outside the reactor 30, and an agitator may be installed therein. 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 mixer 10 via a supply line 50. Thus, the oil separated from the additive via the still 46 is supplied to the mixer 10 through the feed 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).

In the apparatus for producing coke additive having the above-described structure, the mixer 10 has a structure in which the slurry is more effectively stirred and mixed. FIG. 2 illustrates the structure of the mixer according to the present embodiment. Referring to FIG. 2, the structure of the mixer of the present embodiment will be described below.

As shown in FIG. 2, the mixer 10 includes a mixing tank 102 in which coal and a solvent are mixed and mixed, a rotating shaft 104 rotatably installed in the center of the mixing tank, At least one stirring blade 106 installed at intervals along the rotation axis, and a driving unit 108 for rotationally driving the rotation axis.

The mixing tank 102 may have a cylindrical cylinder structure extending in the vertical direction to form a space for receiving coal and a solvent therein. A rotating shaft 104 is extended along the center axis of the mixing tank 102 to be rotatable. A driving unit 108 including, for example, a driving motor is connected to one end of the rotating shaft 104 to rotate the rotating shaft 104 at a predetermined speed.

The stirring shaft 104 is provided with a stirring vane 106 so that the coal and the solvent contained in the mixing tank 102 can be evenly mixed. As shown in FIG. 2, the stirring vane 106 may be installed at a lower end of the rotary shaft 104 and the other may be installed at a position spaced apart from the lower end of the rotary shaft 104 by a predetermined distance. have. The number of the stirring vanes 106 is not limited to two, and may be variously provided depending on the specifications of the equipment and the operating conditions.

The stirring vanes 106 may be formed of, for example, a propeller type, a screw type, or a turbine type impeller.

Accordingly, when the rotary shaft 104 is rotated, the stirring vanes 106 installed on the rotary shaft 104 rotate, so that the coal and the solvent contained in the mixing tank 102 can be stirred more evenly.

The mixer 10 includes a circulation pipe 110 through which a slurry is circulated by connecting a bottom portion and an upper portion of the mixing tank 102 and a circulation pipe 110 installed at one side of the circulation pipe to circulate the slurry in the mixing tank 102 And a circulation pump 112 for stirring.

The circulation pipe (110) is installed by connecting the lower end of the mixing tank (102) and the upper side. Accordingly, when the circulation pump 112 is driven, the slurry mixed in the mixing tank 102 is circulated along the circulation pipe 110. The slurry inside the mixing tank 102 is conveyed to the upper part of the mixing tank 102, for example, through the circulation pipe 110 at the lower end of the mixing tank 102. As a result, the slurry is circulated vertically in the mixing tank 102 and the slurry is mixed with each other.

In this way, by stirring the slurry by the rotation of the stirring vane 106 and circulating the slurry up and down, the stirring efficiency of the slurry can be increased.

As shown in FIG. 2, the mixer 10 may further include a baffle 114 on the inner surface of the mixing tank 102 to increase the stirring efficiency of the slurry and prevent the slurry from accumulating on the inner surface of the mixing tank. The baffle 114 is installed on the inner surface of the mixing tank 102 and extends from the upper portion to the lower portion along the axial direction and protrudes toward the center portion at a predetermined height.

The baffle 114 may be installed on the inner surface of the mixing tank 102 along the circumferential direction with at least one space therebetween. The baffle 114 may be formed so as not to interfere with the stirring vane 106 when the stirring vane 106 installed on the rotating shaft 104 is rotated.

The baffle 114 prevents the slurry from accumulating on the inner circumferential surface of the mixing tank 102 while forming a vortex in the slurry. When the impeller rotates, the slurry rotates in the direction of rotation of the impeller inside the mixing tank. Thus, in the absence of a baffle, the slurry is uniformly rotated in one direction inside the mixing tank, and the possibility that the slurry is fixed to the inner surface of the mixing tank becomes high.

In this embodiment, the baffle 114 is fixed to the inner surface of the mixing tank with respect to the rotating impeller, so that the slurry, which is rotated according to the rotation of the impeller, hits the baffle and forms a vortex. Accordingly, the slurry impinging on the baffle is guided to the impeller located at the center of the mixing tank, thereby increasing the fluidity and minimizing the adherence to the inner surface of the mixing tank.

Hereinafter, a process for producing an additive according to this embodiment will be described.

The process for preparing the additive includes a coal pretreatment process in which coal is dispersed in a solvent to form a slurry, a process of adding a dispersed iron catalyst in coal pretreatment, a coal liquefaction process in which coal slurry is reacted with cracking gas to liquefy coal slurry, A process of supplying COG and / or LNG with a cracking gas during the liquefaction process, a process of separating the additive from the liquefied product, and a recirculation process of supplying the liquid oil obtained in the separation process to the coal pretreatment process and using it as a solvent do.

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 and the solvent supplied to the mixer of this embodiment are effectively stirred and slurried in the mixing tank. In the mixing tank, the slurry is agitated according to the rotation of the stirring blades, and the slurry is circulated up and down through the circulation pipe as the circulation pump is driven.

As described above, the slurry is effectively mixed and mixed in the mixing tank through the stirring wing and the circulation pipe, thereby reducing the stirring time required for mixing the slurry and homogenizing the temperature. Thus, ultimately, the production amount of the additive for coke can be increased.

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 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 mixer 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: mixer 12: crusher
14: dryer 20: catalyst supplier
30: Reactor 32: Gas supply part
40: separator 42: separator
44: Filter device 46: Distiller
50: supply line 102: mixing tank
104: rotating shaft 106: stirring blade
108: driving part 110: circulation pipe
112: Circulation pump 114: Baffle

Claims (7)

A mixer for mixing the pretreated coal and the solvent to form a slurry,
A catalyst supplier for supplying the dispersed iron catalyst to the mixer,
A reactor for liquefying the coal slurry through the mixer,
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 separator and the mixer to supply the oil separated from the separator to the mixer as a solvent,
The mixer includes a mixing tank in which coal and a solvent are mixed and mixed, a rotating shaft rotatably installed in the center of the mixing tank, at least one stirring blade provided on the rotating shaft at intervals along the axial direction, And a drive unit for driving the coke additive. The method according to claim 1,
Wherein the mixer further comprises a circulation pipe for circulating the slurry through a bottom portion and an upper portion of the mixing tank and a circulation pump installed at one side of the circulation pipe for circulating and stirring the slurry in the mixing tank. 3. The method of claim 2,
Wherein the mixer further comprises at least one baffle provided at an interval on the inner circumferential surface of the mixing tank and protruding toward the center portion. The method of claim 3,
Wherein the baffle extends from the top to the bottom along the axial direction of the mixing tank. 5. The method according to any one of claims 1 to 4,
The separator includes a separator for separating a gas component from a 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 separated from the filter device, And a distiller connected to the mixer to supply the additive and the separated oil to the mixer. 6. The method of claim 5,
A pulverizer for pulverizing coal for pretreatment of coal, and a dryer for drying the pulverized coal. 6. The method of claim 5,
Wherein the catalyst supply unit supplies Fe ₂ O ₃ as a dispersed iron catalyst.

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