KR101862151B1 - Tar reforming apparatus and tar reforming method using the same - Google Patents

Abstract

The present invention relates to a tar reforming apparatus for separating and reforming tar among COG (Coke Oven Gas) generated during coke production, characterized in that tar separated from COG is heat-treated to separate the light oil and the mixed oil from the tar using boiling point difference The first tower and the first tower that produce the reformed tar are supplied with the mixed oil. The naphthalene and the absorbing oil contained in the mixed oil are sent upward by using the difference in boiling point, and the tar contained in the mixed oil is sent downward And a third tower for separating the naphthalene and the absorbing oil by using a difference between the boiling point of the naphthalene and the absorbing oil by receiving a mixture of the naphthalene and the absorbing oil from the second tower and the second tower producing the reformed tar.
Therefore, according to the embodiment of the present invention, it is possible to produce an absorbent oil having a content of a component having a high boiling point, which is lower than that of the prior art, and can improve the absorption ability of the absorbent oil. It is possible to reduce the content of naphthalene in the absorption oil, thereby reducing the occurrence of clogging or odor generation due to naphthalene during transportation of the absorption oil.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a tar reforming apparatus and a tar reforming method using the same,

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a tar reforming apparatus and a tar reforming method using the same, and more particularly, to a tar reforming apparatus capable of improving the quality of an absorbing oil as a by-product during tar reforming, and a tar reforming method using the same.

Generally, Coke Oven Gas (COG) is a by-product gas generated during the process of producing coke oven-to-coke pretreated coke. It removes the impurities contained in the gas, .

The coke making plant includes a COG refining apparatus. As shown in the general FIG. 1, a plurality of cokes are mixed and stored in a mixing tank, and a plurality of cokes, that is, (Not shown) for separating the coke oven gas (hereinafter referred to as COG) exhausted or discharged from the coke oven into COG and ordinal water, and an ordinance water separator 31 to separate the coke oven from the coke oven (Not shown) for cooling the COG that has been removed, ammonia is removed from the COG that has been subjected to a desulfurizer or desulfurizer that has a scrubber to remove the sulfide (S), for example, H ₂ S from the cooled COG, A decanter for separating impurities including tar from the ordinal water separated from the COG by a collecting tower for separating and collecting the diesel oil (BTX) from the COG, a decanter And a tar reforming apparatus for reforming the separated tar so as to be used as an additive to be mixed with coking coal and producing an absorption oil for collecting the diesel oil (BTX).

The COG purification process in the above-described coke production facility is as follows. COG of 800 DEG C generated in the coke oven 10 is cooled by the ordination and separated into COG and ordinal water in the ordinate separator. Impurities such as tar, which are heavy in weight, separated from the Ordnox separator, flow into the descender 30 together with the ordination, where the tar and ordinal water are separated by the difference in specific gravity, and the separated tar is moved to the tar reformer And ordination is transferred to the Ordnance Tank and stored respectively. The tar modified in the tar reformer is then used as an additive to be mixed with the raw coal. In the absorption column, BTX is absorbed in the absorbing oil in the COG, the absorption oil is transferred to the distillation column to separate the landscape oil, and the absorption oil in which the landscape oil is separated is distilled off in the separation tower, do.

On the other hand, about 11 wt% to 13 wt% of naphthalene is contained in tar, and naphthalene generates a serious odor and has a property of precipitating and depositing when the temperature is lowered to a certain temperature or lower. However, in order to produce coke, coal and tar are mixed with each other to be carbonized in a coke oven. COG generated at this time contains naphthalene. As described above, the COG is circulated in the COG refining apparatus. At this time, naphthalene contained in the COG causes troubles in the piping, the cooler, and the collecting column to lower the cooling efficiency and the collecting rate. The trapping rate of H ₂ S in the exhaust gas is reduced. And, naphthalene is deposited on the piping or valve that is transported for COG refining, which causes clogging, and this clogging causes problems in the whole equipment.

Therefore, in order to prevent the problem caused by the naphthalene, the naphthalene is removed from the tar reforming apparatus, but the quality of the absorbent oil is low. As described above, the absorbing oil absorbs and captures the light oil (BTX), and the absorbing ability of the light oil (BTX) decreases as the content of a high boiling point component such as naphthalene is large. The low quality of the absorbing oil means that a large amount of the boiling point component of the absorbing oil produced through the tar reforming apparatus is contained.

Korean Patent No. KR 10-0516501 B1

The present invention provides a tar reforming apparatus capable of improving the quality of an absorbing oil produced as a by-product during tar reforming, and a tar reforming method using the same.

TECHNICAL FIELD The present invention relates to a tar reforming apparatus capable of improving the absorption ability of absorbing oil and reducing the problems caused by naphthalene, and a tar reforming method using the same.

The present invention relates to a tar reforming apparatus for separating and reforming tar among coke oven gas (COG) generated during the production of coke, wherein the tar separated from the COG is heat-treated, and the tar- A first tower for separating and producing reformed tar; The naphthalene and the absorbing oil contained in the mixed oil are sent to the upper side together with the mixed oil using the difference in boiling point and the tar contained in the mixed oil is sent downward to separate the mixed tar from the first tower, 2 towers; A third tower for receiving a mixture of the naphthalene and the absorption oil from the second tower and separating the naphthalene from the absorption oil by using a boiling point difference; .

A reformed tar in which the light oil and the mixed oil are separated from the first tower; and a tar tank in which the naphthalene and the reformed tar separated from the absorption oil are stored in the second tower; A naphthalene tank for storing naphthalene separated from the third tower; And an absorption oil tank for storing the absorption oil separated from the third tower.

The first tower sends the light oil, which is contained in the tar before the reforming, to the upper side, sends the mixed oil to the region between the upper and lower ends, and separates the tar to the lower side.

The trough oil moving line having one end connected to the upper end of the first tower so as to move the light oil separated from the first tower to the outside of the first tower; A first tar moving line having one end connected to the lower end of the first tower and the other end connected to the tar tank so as to move the tar reformed in the first tower to the tar tank; A naphthalene and absorbing oil movement line having one end connected to the upper end of the second tower and the other end connected to the third tower so as to move the naphthalene and the absorbing oil separated to the upper side of the second tower to the third tower; And a second tar moving line having one end connected to the lower end of the second tower and the other end connected to the tar tank so as to move the tar reformed in the second tower to the tar tank.

The third tower is configured to send naphthalene separated from the mixture to the upper side, to discharge the absorbing oil to the lower side, to move the naphthalene separated from the third tower to the naphthalene tank, A naphthalene movement line connected to the top and connected at the other end to the naphthalene tank; And an absorbing oil transfer line having one end connected to the lower end of the third tower and the other end connected to the absorbing oil tank so as to move the absorbing oil separated from the third tower to the absorbing oil tank.

And a heater connected to the third tower to reheat the absorbing oil separated from the third tower to re-supply the absorbed oil to the third tower.

A reflux unit is installed at the top of each of the first to third towers.

The tar reforming method according to the present invention is characterized in that the separated tar among the COG (Coke Oven Gas) generated in the coke oven by the coke oven is converted into the coke oven gas and the mixed oil contained in the tar before the reforming using the boiling point difference in the first tower Separating the crude tar and the mixed oil to produce reformed tar separated from the crude oil and the mixed oil; The mixed oil is moved to the second tower and heat treated to move the naphthalene and the absorbing oil contained in the mixed oil upward in the second tower by using a difference in boiling point, To produce reformed tar in which the naphthalene and the absorption oil are separated; And transferring the naphthalene and the absorbing oil to the third tower and performing heat treatment to separate the naphthalene and the absorbing oil using a difference in boiling point to produce an absorbing oil.

In the process of producing the absorbent oil by separating the naphthalene and the absorbent oil from the third tower, the naphthalene is sent to the upper end and the absorbent oil is separated to the lower end.

In the process of producing the reformed tar in which the naphthalene and the absorption oil are separated,

The mixed oil is heat-treated at a temperature of 300 ° C to 350 ° C.

In the process of producing the reformed tar in which the light oil and the mixed oil are separated, the pre-reforming tar is heat-treated at 300 ° C to 350 ° C, and the naphthalene and the absorption oil are separated to produce an absorption oil. And the water-absorbing oil is heat-treated at 230 to 280 캜.

Refluxing the dew condensed oil discharged from the upper part to the inside and outside of the first tower a plurality of times by moving to the upper side of the first tower; Refluxing the naphthalene and the absorbing oil discharged from the upper part to the inside and outside of the second tower plural times so as to flow in and out a plurality of times by moving to the upper side of the second tower; And refluxing the naphthalene discharged to the upper end of the third tower into and out of the second tower a plurality of times.

According to the embodiment of the present invention, it is possible to produce an absorbent oil having a content of a component having a high boiling point which is reduced compared with the conventional one, and the absorbing ability of the absorbent oil can be improved.

In addition, it is possible to reduce the content of naphthalene in the absorption oil, thereby reducing the occurrence of clogging or odor generation due to naphthalene during the movement of the absorption oil.

1 is a schematic view showing a general coke making facility
2 is a conceptual diagram illustrating a tar reforming apparatus according to an embodiment of the present invention.
FIG. 3 is a graph showing the absorption rate of landscape oil of the absorption oil produced as a by-product during tar reforming using the tar reforming apparatus according to the conventional and the present invention,
4 is a graph showing the content of components having boiling points of 290 DEG C or lower among the components contained in each of the absorbent oils produced by the tar reforming apparatus according to the prior art and the embodiment
5 is a graph showing the content of naphthalene contained in each of the absorbent oils produced by the tar reforming apparatus according to the prior art and the embodiment

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. It should be understood, however, that the invention is not limited to the disclosed embodiments, but is capable of other various forms of implementation, and that these embodiments are provided so that this disclosure will be thorough and complete, It is provided to let you know completely.

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a tar reforming apparatus for reforming Tar separated from coke oven gas (COG), which is a by-product in the production of coke in a coke oven. And more particularly, to a tar reforming apparatus capable of increasing the quality of an absorbing oil produced as a by-product during the reforming of tar.

The tar contains about 4 wt% water, 1 wt% to 2 wt% of tartaric acid, 5 wt% of wash oil, 11 wt% to 13 wt% of naphthalene, 35 wt% of 40 wt% of creosote (creosote) and a pitch of 35 wt% to 40 wt%. Describing the components contained in tar as an elemental component, it contains a component system consisting of 92.6 wt% of C, 5.15 wt% of H, 0.96 wt% of 0.96, 0.75 wt% of S and unavoidable impurities.

Here, the H of the aromatic hydrocarbon contained in the tar lowers the softening start temperature of the raw coal and improves the cohesiveness of the raw coal. On the other hand, the tar acids, the absorption oil, the naphthalene, the creosote, and the pitch contained in the tar are different from each other in boiling point, This is the pitch.

A tar reforming apparatus according to an embodiment of the present invention provides a tar reforming apparatus and a tar reforming method that prevent occurrence of problems due to naphthalene and improve the quality of absorbed oil. In particular, the present invention aims to improve the absorbing ability of diesel light oil by reducing the component content of the absorbing oil having a boiling point higher than 290 deg.

The naphthalene and the absorbing oil are separated from the tar. At this time, the absorbing oil is separated so that the content of the component having a boiling point higher than 290 占 폚 is lower than that of the conventional one.

Hereinafter, a tar reforming apparatus according to an embodiment of the present invention will be described with reference to FIG.

2 is a conceptual diagram illustrating a tar reforming apparatus according to an embodiment of the present invention.

Referring to FIG. 2, a tar reforming apparatus according to an embodiment of the present invention includes:

A dehydration tower 110 for removing or separating water (or moisture) from tar provided from a tar tank in which tar is stored before reforming (hereinafter referred to as first tar tank 40), a light oil A first tower 121 for separating mixed oil from the first tower 121 and a first material containing naphthalene and absorbing oil contained in the mixed oil by receiving mixed oil from the first tower 121, A second tower 122 separating into a second material, a third tower 123 separating the naphthalene and the absorbing oil supplied from the second tower 122, a naphthalene and an absorbing oil separated from the third tower 123, The naphthalene tank 320 and the absorption oil tank 330 that store the tars, the tar tank that stores the tar separated from the first tower 121 and the second tower 122, that is, the tar tar (hereinafter referred to as the second tar tank 310). The first to third heaters 500, 700, and 800 are connected to the first to third towers to provide a heat source for separating the object to be treated.

The tar reforming apparatus 1000 includes first to third refluxers 510, 520 and 530 connected to the upper ends of the first to third towers 121, 122 and 123, a dewatering tower 110, A water separator 410 connected to each of the first towers 121 to receive water vapor from the dewatering tower 110 and diesel oil moved from the first tower 121 to separate water and landscaping passage, And a light oil tank 420 for storing light oil.

And, for the movement of the raw materials between the above-described structures, a moving line is provided between each interlocked structure, which provides a moving path or passage through which the raw material can move. That is, the tar reforming apparatus 1000 includes a first moving line 1 for connecting the dewatering tower 110 and the water separator 410, a second moving line 1 for connecting the dewatering tower 110 and the first heater A third moving line 3 connecting the first heater 500 and the first tower 121, a fourth moving line 4 connecting the steam supplier 600 and the first tower 121, A fifth moving line 5 connecting the first tower 121 and the water separator 410, a sixth moving line 6 connecting the water separator 410 and the tank tank 420, A seventh transfer line (or first tar transfer line) 7 for connecting the tower 121 and the second tar tank, an eighth transfer line (or a mixer) for connecting the first and second towers 121 and 122, A ninth moving line 9 for connecting the second tower 122 and the second heater 700 and a ninth moving line 9 for connecting the upper end of the second tower 122 and the third tower 123, 10 transfer line (or naphthalene and absorption oil transfer line, 10), a second transfer line An eleventh moving line (or a second tar moving line) 11 for connecting the first tank 122 and the second tar tank 310, a twelfth moving line (Or a naphthalene moving line 13) connecting the third tower 123 and the naphthalene tank 320, a third tower 123 and an absorbing oil tank 330 connecting the third tower 123 and the naphthalene tank 320, One end is connected to the second tar tank 310 and the other end is connected to the second transfer line 2 so as to be connected to the second tar tank 310 And a fifteenth transfer line 15 for supplying the stored reformed tar to the first heater 500. [

Each of the first to fifteenth movement lines 1 to 14 may be in the form of a pipe extending in at least one direction and having an inner space.

Each of the first to third towers 121, 122 and 123 is a kind of distillation column for separating and separating the object to be treated mixed with a plurality of substances by boiling point difference. To this end, heaters 500, 700, and 800 are connected to the first tower 121, the second tower 122, and the third tower 123, respectively.

The tar from which the water is removed by the dehydration tower 110 is tar before the reforming and the tar separated from the first and second towers 121 and 121 is the reformed tar. In the second tower 122, The oil tarred tar is modified tar.

As described above, each of the dehydration tower 110, the first tower 121, the second tower 122, and the third tower 123 is a kind of distillation tower for separating the raw materials using the boiling point difference. Each of the dehydration tower 110, the first tower 121, the second tower 122, and the third tower 123 has a similar configuration and shape. Briefly, the dewatering tower 110, the first tower 121, the second tower 122 and the third tower 123 each have a body having an internal space and a plurality of openings And the plurality of partition plates are vertically spaced apart from each other in the main body. In each of the towers 110, 121, 122, and 123, the raw materials are separated due to the difference in boiling point. Due to their specific gravity, the lower the boiling point, the more the material moves upward. Conversely, the higher the boiling point, the lower the material is. At this time, the materials move through the openings of each of the plurality of partition plates.

The dehydration tower 110 is a means for removing water (moisture) contained in tar by receiving tar reformed before being separated by the decanter 30 and stored in the tar tank 40. On the other hand, when tar is stored in the first tar tank 40 before reforming or dehydration, the tar is supplied to the dehydration tower 110 while being maintained at a temperature of 70 ° C to 100 ° C to prevent the tar from solidifying .

When the tar of the first tar tank 40 is moved to the dewatering tower 110, it is heated to 110 to 180 DEG C by means of a heat exchanger, a heater or the like in a pipe connecting the dewatering tower 110. [ In the dehydration tower 110 according to the embodiment, the tar and water contained in the tar are separated using a difference in boiling point. That is, in the dehydration tower 110, the pre-reforming tar is heated to a temperature equal to or higher than the boiling point of water and less than the boiling point of tar, and the water contained in the tar is in the form of water vapor. Since the water vapor is light in weight, it moves to the upper side of the dehydration tower 110, and the relatively heavy tar goes down to the bottom.

The first movement line 1 is connected to connect the upper end to the dewatering tower 110 and the water separator 410 and the second movement line 1 is connected to the lower end of the dewatering tower 110 and the first heater 500, Line 2 is connected.

The first heater 500 heats the tar provided from the dewatering tower 110 to 300 ° C to 350 ° C and supplies the tar to the first tower 121. That is, the tar heated at 300 ° C to 350 ° C in the first heater 500 is supplied to the first tower 121 through the third transfer line 3. The first heater 500 may be a means including a container having an inner space capable of receiving tar and a heating unit for heating the container or tar. The heating unit may be any means that can heat the container or the tar.

The first tower 121 separates the light oil and the mixed oil from the pre-reforming tar which is separated from the water to produce the modified tar. That is, when the pre-reforming tar heated to 300 ° C to 350 ° C by the first heater 500 is supplied to the first tower 121, depending on the boiling point in the first tower 121, The oil is separated. In other words, it is separated into the light oil, the mixed oil and the reformed tar in the first tower 121. That is, when the tar is heated to 300 ° C. to 350 ° C. before the reforming and supplied to the first tower 121, the light oil and the mixed oil are separated from the tar before the reforming due to the difference in boiling point. . At this time, the lowest light oil having a boiling point of less than 200 deg. C is vaporized and moves upward in the first tower 121, and the boiling point is, for example, higher than 330 DEG C, . The mixed oil having a boiling point of 210 ° C or higher and lower than 330 ° C is collected in the first tower 121 between the upper and lower spaces or between the space where the landscape oil and the tar gather. The mixed oil is an oil mixed with naphthalene, absorbing oil and tar, and the absorbing oil is a liquid in the form of a mixture composed of components having a boiling point higher than that of naphthalene (i.e., 230 to 330 ° C). The tar contained in the mixed oil is mostly tar having a boiling point of 330 ° C or less. That is, in the first tower 121, crude oil, a mixed oil including tar having a boiling point of 330 ° C or lower, and tar having a boiling point exceeding 330 ° C are separated. Then, the mixed-tar tar is moved to the second tower 122 and then reformed again.

In order to separate the light oil, the mixed oil and the tar from the first tower 121, steam is supplied in order to increase the separation efficiency. To this end, a fourth transfer line 4 is connected between the first tower 121 and the steam supply 600, and steam is supplied to the first tower 121.

A fifth moving line 5 is connected to the upper end of the first tower 121 and is connected to the outside of the first tower 121. The lower end of the first tower 121 And a seventh transfer line 7, which is a passage through which tar, that is, the tar tar, is separated. An eighth movement line 8, which is a passage through which the mixed oil moves, is connected to the center side portion between the upper end and the lower end of the first tower 121, for example, the vertical center of the first tower 121. Therefore, the light oil separated from the first tower 121 goes up to the upper part of the first tower 121, moves to the water separator 410 through the fifth transfer line 5, and the tar having the highest boiling point flows through the first And moves to the second tar tank 310 through the seventh transfer line 7 connected to the lower end of the tower 121. The mixed oil moves to the second tower 122 through the eighth movement line 8 that is cut between the upper end and the lower end of the first tower 121 (side cut).

Here, the tar discharged from the lower end of the first tower 121 is tar (or reformed tar) that has undergone the reforming treatment since the light oil and the mixed oil are separated or removed, and this tar is transferred to the second tar tank.

On the other hand, the water vapor separated from the dehydration tower 110 may include landscape oil, and conversely, the landscape oil separated from the first tower 121 may include water vapor. Therefore, the water vapor separated from the dehydration tower 110 and each of the light oil separated from the first tower 121 are transferred to the water separator 410, where the water and the light oil are separated. The separated diesel oil is transferred through the sixth transfer line 6 and stored in the light oil tank 420.

In the second tower 122 according to the embodiment of the present invention, the mixed oil is separated into two types, namely, naphthalene and absorbent oil as the first material and tar as the second material. More specifically, the mixed oil includes naphthalene, absorption oil, and tar. In the second tower, the mixed oil is not classified into three types (naphthalene, absorbent oil and tar), and the naphthalene and the first material It is separated into two kinds by the second material of tar and tar. To this end, the second heater (700), which will be described later, is used to heat the interior of the second tower (122) or the mixed oil to 300 ° C to 350 ° C.

In the embodiment, both the separating second material, naphthalene and the absorbing oil, are moved upward in the second tower and separated from the tar. In other words, the naphthalene, the absorbing oil, and the absorber having a boiling point between the naphthalene and tar among the tar are collected separately in the region between the upper end and the lower end of the second tower 122, The absorbing oil is moved to the upper side in the second tower 122 at the same time or together. To this end, the moving lines 10 and 11 are connected to the upper and lower ends of the second tower 122, respectively, and no separate moving line is connected to the upper and lower ends. That is, the tenth moving line 10 is connected to the upper end of the second tower 122 to separate the naphthalene and the absorbing oil into the upper part of the second tower 122 and the lower part of the tar, And the moving line is not connected between the upper end and the lower end of the second tower 122 as in the prior art.

The naphthalene and the absorbing oil separated from the second tower 122 are transferred to the third tower 123 through the tenth transfer line 10 and the tar is transferred through the eleventh transfer line 11 to the second tank Lt; RTI ID = 0.0 > 310 < / RTI >

In the second tower 122, both the naphthalene and the absorbing oil are gathered at the upper side to separate the absorbing oil and the tar more accurately. In other words, more specifically, the content of the component having a boiling point of 290 ° C or higher than that of the tar included in the absorbent oil is reduced compared with the conventional one. The reflux machine 520 installed at the upper end of the second tower 122 cools the naphthalene and the absorbing oil discharged through the supercharger of the second tower 122 into a liquid phase and supplies it to the second tower 122, 2 tower 122 functions to reflux again so that separation due to a difference in boiling point occurs. In other words, reflux occurs in which the naphthalene and the absorption oil repeatedly flow in and out of the interior and the exterior of the second tower a plurality of times by the reflux condenser 520, thereby separating the naphthalene and the tar from the absorption duct in the second tower 122 Is performed plural times or plural times. Therefore, the amount of tar containing the boiling point of 290 DEG C or higher in the absorbing oil can be reduced or not included in comparison with the conventional case.

On the other hand, between the upper and lower ends of the second tower 122, for example, on the side of the second tower 122, it is difficult or impossible to install the reflux machine due to its structure. Conventionally, a moving line is connected to the upper and lower ends of the second tower 122 and the side between the upper and lower ends, respectively, to separate naphthalene as the upper end of the second tower 122, tar as the lower end and tar oil as the side . However, since the reflux can not be installed on the side of the tower as described above, the naphthalene is refluxed a plurality of times into the second tower by the reflux machine provided at the upper end of the second tower, but the absorption oil is not refluxed, Tar, especially tar having a boiling point of 290 DEG C or more may be present in a large amount, thereby lowering the absorption rate of diesel oil.

In addition, it is preferable that the second tower 122 according to the embodiment has a smaller height than the conventional second tower 122, and the number of the partition plates or the interval between them is reduced. This is to reduce the energy for raising the naphthalene and the absorbing oil upward in the second tower 122 by the boiling point temperature.

The second heater 700 provides a heat source to the second tower 122 to separate the blended oil into naphthalene and absorbent oil and tar. Where the heat source may be in fluid form and travels through the ninth transfer line 9 to the second tower 122 to heat the interior of the second tower 122 or the blended oil. The second heater 700 according to the embodiment is a means having a heat exchange function such as a boiler, but is not limited thereto. Various means capable of providing a heat source to the second tower 122 are applicable.

The third tower 123 separates the first material supplied from the second tower 122 in a state where the naphthalene and the absorption oil are mixed, from the naphthalene to the absorption flow passage. That is, in the third tower 123, the naphthalene having a boiling point of 210 ° C to 220 ° C and the boiling point of 220 ° C to 330 ° C are separated. To this end, the third heater 800, which will be described later, is used to heat the inside of the third tower or the naphthalene and the absorbing oil to 300 to 350 ° C.

In the third tower 123 according to the embodiment, the naphthalene and the absorbing oil are separated into the upper and lower ends of the third tower 123, respectively. Namely, the naphthalene or absorbing oil is separated into the upper and lower ends of the third tower 123, not on the upper and lower ends of the third tower 123 but on the area between the upper and lower ends of the third tower 123. At this time, the naphthalene having a low boiling point is moved upward in the third tower 123 and moved downward in the third absorption tower 123 having a boiling point higher than that of naphthalene.

A reflux condenser 530 is connected to the upper end of the third tower 123 and the naphthalene is repeatedly introduced into the third tower 123 and discharged to the outside by the reflux machine 530 a plurality of times At this time, the separation between the naphthalene and the absorbing oil is repeated plural times within the third tower 123. Therefore, naphthalene can produce an absorbent oil having a smaller content than the conventional one.

The naphthalene moved upward in the third tower 123 is moved to and stored in the naphthalene tank 320 through the thirteenth moving line 13. The absorbed oil moved downward in the third tower 123 14 moving line 14 to the absorption oil tank 330 and stored.

The third heater 800 provides a heat source to the third tower 123 to separate the naphthalene and absorbing oil. In the third heater according to the embodiment, the absorbing oil discharged from the lower end of the third tower 123 is reboiled or reheated, and then supplied to the third heater 800, whereby the separation efficiency of naphthalene Can be improved.

Thus, according to the embodiment of the present invention, the naphthalene and the absorbing oil are separated from the second tower 122 to the upper side or the upper side in the second tower 122. At this time, as the naphthalene and the absorbing oil are refluxed into the second tower 510 a plurality of times by the refluxer 510 connected to the upper end of the second tower 122, the process of separating the naphthalene and the absorption channel from the tar is performed a plurality of times . Therefore, in the second tower 122, the separation between the tar having a boiling point of 290 DEG C or higher and the absorbing oil is made more accurate than in the prior art, and the content of tar contained in the absorbing oil can be reduced. That is, it is possible to produce an absorbent oil having a low content of components having a boiling point of 290 ° C or higher.

In the third tower 123 provided separately from the second tower 122, the first material, which is a mixture of the absorbent oil and naphthalene, is separated into the absorbent oil and the naphthalene. Therefore, the content of naphthalene, which has a low boiling point, Low absorption oil can be produced.

Hereinafter, the operation of the tar reforming apparatus and the tar reforming method according to the embodiment of the present invention will be described with reference to FIGS. 1 and 2. FIG. At this time, the contents overlapping with those described above will be omitted or briefly explained.

The COG discharged through the riser of the coke oven 10 separates the tar (tar before the reforming) from the descender 30 and the COG from which the tar has been separated passes through the desulfurizer 50 to separate and remove H ₂ S (BTX) is separated from the COG using the absorption oil in the absorption column 60 and collected.

The tar separated from the COG is stored in the first tar tank and is reformed through the tar reforming apparatus according to the embodiment, and the absorption oil is produced as a by-product.

That is, the tar stored in the first tar tank 40 is maintained at 70 ° C to 100 ° C to prevent solidification, and then moved to the dehydration tower 110 while being heated to have a temperature of 110 ° C to 180 ° C. When the tar is heated to a temperature of 110 ° C to 180 ° C which is the boiling point of water, the water contained in the tar is vaporized. When the tar is supplied to the dehydration tower, the water vapor moves to the upper side of the dehydration tower 110 and is separated. The steam is transferred to the water separator 410 through the first transfer line 1 and the tar removed from the water is supplied to the first heater 500 through the second transfer line 2.

In the first heater 500, the tar removed from the water is heated to 300 ° C. to 350 ° C. and supplied to the first tower 121. In order to increase the separation efficiency, the steam generated in the steam generator 600 is supplied to the first tower 121 121).

When tar and steam heated to 300 ° C to 350 ° C are supplied into the first tower 121, the light oil and the mixed oil contained in the tar are separated by the difference in boiling point. That is, as the tar before the reforming is heated to 300 ° C to 350 ° C, the low-temperature conditioning oil having a boiling point of 200 ° C or lower from the pre-reforming tar is vaporized and separated from the pre-reforming tar, Move. The mixed oil, which is a substance having a boiling point of 210 ° C. or more and 330 ° C. or less, is separated from the tar before the reforming and is separated into a space between the upper end and the lower end in the first tower 121, Gather. Here, the separated mixed oil contains naphthalene, absorbent oil and tar, and the tar included in the mixed oil is mostly tar having a boiling point of 290 ° C or higher and 330 ° C or lower.

The tar (reformed tar) from which the diesel oil and the mixed oil are separated is a tar having a boiling point exceeding 330 DEG C and is discharged through the lower end of the first tower 121 and is discharged through the seventh transfer line 7 to the second And stored in the tar tank 310.

The diesel oil moved to the upper side of the first tower 121 moves to the water separator 410 through the fifth moving line 5. The water separator 410 separates the light oil and the water, and the produced light oil is stored in the light oil tank 420.

The mixed oil separated from the first tower 121 is moved to the second tower 122. In the second tower 122, naphthalene and absorption oil as the first material and tar as the second material are separated. To this end, the second heater (700) is operated to heat the second tower (122) to 300 ° C to 350 ° C. Among the components contained in the mixed oil, naphthalene and the absorbing oil migrate upward in the second tower 122 and are separated. The naphthalene and the oil in which the absorbing oil is separated, that is, the boiling point of 290 DEG C or more and 330 DEG C or less The tar (reformed tar) moves downward in the second tower 122 and is stored in the second tar tank 310.

As described above, the separated naphthalene and absorbing oil are moved upward to be discharged from the upper end of the second tower 122, connected to the upper end of the second tower 122, 2 tower 122 and out of the tower 122 a plurality of times. Thus, the tablets separating naphthalene and tar from the absorption channel are repeated a plurality of times, so that the content of tar in the naphthalene and the absorption oil can be reduced as compared with the conventional one.

The reformed tar separated to the lower end of the second tower 122 is moved to and stored in the second tank tank 310 through the eleventh transfer line 11. The naphthalene and the absorbing oil separated at the upper end of the second tower 122 move through the tenth moving line 10 and are supplied to the third tower 123.

In the third tower 123, a mixture of naphthalene and the absorption oil separated from the second tower 122 is separated from the naphthalene and the absorption flow path. To this end, the third tower 123 is heated to 230 ° C. to 280 ° C. by using the third heater 800, so that naphthalene having a low boiling point is moved upward in the third tower 123, The tar having a high boiling point moves to the lower side in the third tower 123. The naphthalene is repeatedly introduced into the third tower 123 and discharged to the outside a plurality of times by the reflux machine connected to the upper end of the third tower 123. At this time, The oil separation is repeatedly performed a plurality of times. Therefore, an absorption oil having a low content of naphthalene is produced.

The naphthalene moved upward in the third tower 123 is moved to and stored in the naphthalene tank 320 through the thirteenth traveling line 13 and the absorbed oil moved downward in the third tower 123 is moved Is transferred to the absorption oil tank through line (14) and stored.

As described above, according to the embodiment of the present invention, the naphthalene and the absorbing oil are separated from the second tower 122 by being sent to the upper side or the upper side of the second tower 122. At this time, as the naphthalene and the absorbing oil are refluxed into the second tower 122 a plurality of times by the refluxer 510 connected to the upper end of the second tower 122, the process of separating the naphthalene and the absorption channel from the tar is performed a plurality of times . Therefore, in the second tower 122, the separation between the tar having a boiling point of 290 DEG C or higher and the absorbing oil is made more accurate than in the prior art, and the content of tar contained in the absorbing oil can be reduced. That is, it is possible to produce an absorbent oil having a low content of components having a boiling point of 290 ° C or higher.

In the third tower 123 provided separately from the second tower 122, the mixture of the absorption oil and the naphthalene is separated into the absorption oil and the naphthalene. Therefore, the absorption oil having a low content of naphthalene, which lowers the boiling point, Can be produced.

FIG. 3 is a graph showing absorption rates of oil of landscape oil of an absorption oil produced as a by-product during tar reforming using each of the tar reforming apparatuses according to the prior art and the present invention. Here, the conventional tar reforming apparatus has a dehydration tower, first and second towers, and does not have a third tower. Then, a moving line is connected to each of the upper and lower ends of the second tower, and the side portions between the upper and lower ends, and heat treatment is performed at about 280 DEG C to separate naphthalene, absorbing oil and tar from the mixed oil. Namely, the absorbing oil is separated into naphthalene to the upper end of the second tower, tar to the lower end, and side portions between the upper end and the lower end.

Then, the absorption rates of the light oil dyes in the absorption oil produced by the conventional tar reforming apparatus (hereinafter referred to as conventional absorption oil) and the absorption oil according to the embodiment of the present invention (hereinafter referred to as the absorption oil according to the embodiment) were confirmed. Referring to FIG. 3, the conventional absorbent oil can absorb 1.9 g of light oil for 100 g of the same amount, but the absorbent oil according to the embodiment of the present invention can absorb 2.3 g. That is, the absorbency of the vegetable oil according to the example was improved by 18% as compared with the conventional case.

FIG. 4 is a graph showing the contents of components having boiling points of 290 ° C. or lower among the components contained in each of the absorbent oils produced by the tar reforming apparatus according to the prior art and the present invention.

Referring to FIG. 4, the content of the conventional absorbent oil having a boiling point of 290 ° C or less is 82% by weight based on the total amount of the absorbent oil, and the absorbent oil according to the embodiment is 96%. The absorbing oil has a better absorbing ability as the content of the component having a boiling point of 290 ° C or higher is smaller, so that it can be seen from FIG. 5 that the absorption ability of the absorbing oil according to the embodiment is good.

5 is a graph showing the content of naphthalene contained in each of the absorbent oils produced by the tar reforming apparatus according to the prior art and the embodiment. Referring to FIG. 5, the conventional absorbent oil contains naphthalene of 3.8 wt%, while the absorbent oil of the present embodiment contains 1.6 wt% of naphthalene. From this, it can be seen that naphthalene which causes clogging of pipes is less contained in the absorbent oil according to the embodiment, and it can be seen that the use of the absorbent oil according to the embodiment is advantageous for safety.

110: Tall tower 121: First tower
122: second tower 123: third tower

Claims (12)

A tar reforming apparatus for separating and reforming tar among COG (Coke Oven Gas) generated during coke production,
A first tower for heat treating the tar separated from the COG to separate the light oil and the mixed oil from the tar using boiling point difference to produce reformed tar;
The naphthalene and the absorbing oil contained in the mixed oil are sent to the upper side together by using the boiling point difference to receive the mixed oil from the first tower and the tar contained in the mixed oil is separated to be sent downward to produce reformed tar 2 towers;
A third tower for receiving a mixture of the naphthalene and the absorption oil from the second tower and separating the naphthalene and the absorption oil from each other using boiling point difference;
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A reformed tar in which the light oil and the mixed oil are separated from the first tower; and a tar tank in which the naphthalene and the reformed tar separated from the absorption oil are stored in the second tower;
A naphthalene tank for storing naphthalene separated from the third tower; And
An absorption oil tank for storing the absorption oil separated from the third tower;
Containing Tar reformer. delete The method according to claim 1,
Wherein the first tower sends the diesel light oil contained in the tar before the reforming to the area between the upper end and the lower end and sends the tar downward to separate the mixed oil. The method of claim 3,
A trough oil moving line having one end connected to the upper end of the first tower so as to move the light oil separated from the first tower to the outside of the first tower;
A first tar moving line having one end connected to the lower end of the first tower and the other end connected to the tar tank so as to move the tar reformed in the first tower to the tar tank;
A naphthalene and absorbing oil movement line having one end connected to the upper end of the second tower and the other end connected to the third tower so as to move the naphthalene and the absorbing oil separated to the upper side of the second tower to the third tower; And
A second tar moving line having one end connected to the lower end of the second tower and the other end connected to the tar tank so as to move the tar reformed in the second tower to the tar tank;
The tar reforming apparatus comprising: The method of claim 4,
The third tower sends naphthalene separated from the mixture upward, separates the absorbing oil downward,
A naphthalene moving line having one end connected to the upper end of the third tower and the other end connected to the naphthalene tank so as to move the naphthalene separated from the third tower to the naphthalene tank;
An absorption fluid line connected at one end to the lower end of the third tower and at the other end to the absorption oil tank so as to move the absorption oil separated from the third tower to the absorption oil tank;
The tar reforming apparatus comprising: The method of claim 5,
And a heater connected to the third tower for reheating the absorbing oil separated from the third tower to re-supply the absorbed oil to the third tower. The method according to any one of claims 1 to 7,
And a reflux unit is installed at an upper end of each of the first to third towers. Separating the separated tar in the COG (Coke Oven Gas) generated in the coke oven by the boiling point difference in the first tower, separating the light oil and the mixed oil contained in the tar before reforming, The process of producing oil tar separated reformed tar;
Moving the mixed oil to the second tower and performing heat treatment to move the naphthalene and the absorbing oil contained in the mixed oil upward in the second tower by using a difference in boiling point, To produce reformed tar in which the naphthalene and the absorption oil are separated;
Transferring the mixture containing the naphthalene and the absorbing oil to the third tower and performing heat treatment to separate the naphthalene and the absorbing oil from the mixture using boiling point difference to produce absorbing oil;
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In the process of producing the reformed tar in which the naphthalene and the absorption oil are separated,
Wherein the mixed oil is heat-treated at a temperature of 300 ° C to 350 ° C. The method of claim 8,
In the process of producing the absorbent oil by separating the naphthalene and the absorbent oil from the third tower,
The naphthalene is sent to the upper end, and the absorbing oil is sent to the lower end to separate the tar. delete The method of claim 9,
In the process of producing the reformed tar in which the light oil and the mixed oil are separated, the pre-reformed tar is heat-treated at 300 ° C to 350 ° C,
In the process of producing the absorbent oil by separating the naphthalene and the absorbent oil,
Wherein the naphthalene and the absorbent oil are heat-treated at 230 to 280 캜. The method of claim 9,
Refluxing the dew condensed oil discharged from the upper part to the inside and outside of the first tower a plurality of times by moving to the upper side of the first tower;
Refluxing the naphthalene and the absorbing oil discharged from the upper part to the inside and outside of the second tower plural times so as to flow in and out a plurality of times by moving to the upper side of the second tower; And
Refluxing the naphthalene discharged to the upper end of the third tower into and out of the second tower a plurality of times;
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