WO2018030584A1

WO2018030584A1 - Process for producing modified tar

Info

Publication number: WO2018030584A1
Application number: PCT/KR2016/012183
Authority: WO
Inventors: 박경태; 김병일; 이승재
Original assignee: 주식회사 포스코
Priority date: 2016-08-08
Filing date: 2016-10-27
Publication date: 2018-02-15
Also published as: CN109790469A; KR101797134B1; EP3498805A4; EP3498805A1

Abstract

The present invention relates to a process for producing modified tar, and can provide a process for producing modified tar, comprising: a first distillation step of removing water and/or a first light oil, of which the boiling point is from 180°C to the boiling point of naphthalene, or lower, by distilling tar, which is a by-product of a cock process, at a temperature from 100°C to a temperature from 180°C to the boiling point of naphthalenein, or lower, in a first distillation tower; a second distillation step of respectively separating modified tar, a second light oil of which the boiling point is lower than that of naphthalene, and a mixed oil comprising naphthalene, wash oil, and modified tar by distilling the product, from which water and/or the first light oil was removed in the first distillation step, at 300-350°C in a second distillation tower; and a third distillation step of respectively separating naphthalene, the mixed oil, and the modified tar by distilling, at 220-260°C in a third distillation tower, the mixed oil of the product of the second distillation step.

Description

【Specification】

[Name of invention]

Modified Tar Production Process

Technical Field

The modified tar production process.

[Technique to become background of invention]

Steel mills produce large quantities of water in blast furnaces. Coal and iron ore as raw materials are required for the production of molten water, and the processing of coal and iron ore directly into the blast furnace causes problems such as breathability. Specifically, coal is converted into coke and iron ore is converted into sintered or pellets and then charged into the blast furnace. In particular, the coke serves to improve ventilation and supply heat sources in the blast furnace, and the coke is produced by coking coal for coke at a high temperature in the coke Aubon. Coal coal from ships or trains is crushed and blended to reduce particle size and match the ingredients in the blending bin. The blended coal is charged into a coke oven and converted into coke after drying. The coke oven is composed of a number of independent combustion chambers and carbonization chambers, and the combustion chamber supplies energy to the carbonization chamber by coke oven gas (COG) combustion, and coal drying occurs in the carbonization chamber.

When carbonization is carried out in the carbonization chamber, volatile components contained in coal exit gaseous coke through a riser in the form of gas. This is called coke oven gas (COG) and is an important energy source in steel mills. The crude coke oven gas is also referred to as Crude COG. Crude COG is refined through desulfurization and various scrubbers to remove sulfur to become C0G used in steel mills. Crude COG is a tar and a heavy tar that precipitates after passing through the Tar Decanter. Tar, a byproduct of the coke process, is stored in storage tanks for sale.

The coke input to the blast furnace is an important indicator of coke quality. Low strength is important to keep the strength high as the coke may break and cause problems in blast furnaces and transfers. If the strength is higher, the quality of coal is lower than that of coke coal. To reduce costs. Many steel mills are making great efforts to improve the strength of coke.

In addition, in the past, attempts to increase the strength by mixing Tar with coke coal have occurred, but when the Tar is used as it is, post-process piping clogging due to triangular odor and naphthalene was generated. To prevent this, a method of preparing coal caking supplements was devised by removing only the malodorous parts. However, the above method has a disadvantage in that naphthalene removal equipment must exist in the COG purification process.

[Content of invention]

Problem to be solved

Tar, a byproduct of the coke process, removes the odorous ^' light oil ^' , and naphthalene, which causes pipe clogging in the process after the coke process. The present invention aims to provide a modified tar production process that can improve the side effects of caking additives.

Furthermore, the light oil separated through the reforming tar production process may be used as fuel or sold, naphthalene may be sold separately, and absorbent oil may be used in the chemical conversion process, thereby improving economic efficiency.

[Measures of problem]

One embodiment of the present invention, by distilling tar (Tar) by-product of the coke process in a U distillation tower above 100 ^° C (180 ^° C ~ boiling point of naphthalene), water and / or boiling point (180 a first distillation step, wherein the first distillate and / or the first light oil in step (Light Oi l) the removed result of it or less ^° the boiling point of C ~ naphthalene) raises the first light oil (Light Oi l) the Distillation at 3001 or higher and 350 ^° C or lower in a distillation tower, the second light oil having a boiling point lower than that of naphthalene; Separation of the mixed oil containing naphthalene, the absorbent oil and the modified Tar and the modified Tar, respectively, is carried out in the second distillation step, and the mixed oil (Mixed Oi l) is the third product of the second distillation step. Distillation at 220 ^° C. or more and 260 ^° C. or less in a distillation tower, the third distillation step of separating the naphthalene absorbent oil, and the modified Tar, respectively, provides a modified tar (Tar) production process.

In the second distillation step, the resultant from which water and / or the first light oil is removed in the first distillation step is 300 ^° C or more and 350 ^° C or less. It could be heated and transferred to the two distillation towers.

In the third distillation stage, mixed oil (Mixed Oil) of the result of the second distillation stage may be transferred to the third distillation tower without additional heating.

It may be to recycle the modified tar (Tar) separated from the second distillation tower and / or the crab triple stream tower, to the second distillation tower. In the second distillation step, it may be to supply steam to the second distillation tower.

After the system 3 distillation step, after re-heating (reboi 1 ing) the reforming tar (Tar) separated in the three distillation step through a heater, further comprising the step of re-input to the crab 3 distillation tower. I can see.

In the second distillation step, the water from which the first distillation step and / or the first light oil (Light Oi l) are removed, and the recycled second distillation tower and / or the third distillation tower The separated modified tar may be heated to 300 ^° C. or more and 350 ^° C. or less, and then introduced into a distillation tower.

Before the first distillation step, it may further comprise the step of heating the tar (Tar) by-product of the coke process through a heat exchanger or a heater to be introduced into the first distillation tower.

The modified tar may be for caking fillers to be added to the coke manufacturing process.

【Effects of the Invention]

Tar is a byproduct of the coke process. Light Oi l, a odorous substance, and naphthalene, which causes pipe clogging, are removed from the coke process. Provides a modified tar production process that can improve the side effects of complementary materials.

Furthermore, the light oil separated through the reforming tar production process may be used or sold as fuel, naphthalene may be sold separately, and the absorbent oil may be used in the chemical conversion process, thereby improving economic efficiency.

[Brief Description of Drawings]

1 can be used in the modified tar production process of one embodiment of the present invention Exemplary schematic diagram of a device present.

[Specific contents to carry out invention]

Hereinafter, embodiments of the present invention will be described in detail. However, this is presented as an example, whereby the present invention is not limited and the present invention is defined only by the scope of the claims to be described later.

The terms first, second, and crab 3 are used to describe various parts, components, regions, layers, and / or sections, but are not limited to these. These terms are only used to distinguish one part, component, region, layer or section from another part, component, region, layer or section. Accordingly, the first part, component, region, layer or section described below may be referred to as crab 2 component, region, layer or section without departing from the scope of the invention.

The terminology used herein is for reference only to specific embodiments and is not intended to limit the invention. As used herein, the singular forms “a,” “an,” and “the” include plural forms as well, unless the phrases clearly indicate the opposite. As used herein, the meaning of "comprising ¹ " specifies a particular characteristic, region, integer, step, operation, element and / or component, and the presence of another characteristic, region, integer, step, operation, element and / or component. I do not exclude wealth.

Although not defined otherwise, all terms including technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. Commonly defined terms used are additionally interpreted to have a meaning consistent with the related technical literature and the presently disclosed contents, and are not interpreted in an ideal or very formal sense unless defined. One embodiment of the present invention, to provide a process for producing a modified tar by modifying the tar (Tar) added as a caking additive for the quality improvement of the coke in the coke (Coke) manufacturing process. Specifically, in the tar which is a by-product of the conventional coke process, light oil, which is a odorous substance, and naphthalene which causes clogging in the process after the coke process are removed, The present invention aims to provide a modified tar production process that can improve the side effects of existing tar caking preservatives. More specifically, one embodiment of the present invention, by distilling tar (Tar), a by-product of the coke process at 100 ^° C or more (boiling point of 180 ^° C naphthalene) in a crab 1 distillation tower, water and / or boiling point The first distillation step of removing the first light oil (Light Oi l) of less than (180 ^° C ~ boiling point of naphthalene), the water and / or crab 1 light oil (Il) is removed in the first distillation step Distillation of the resultant in a second distillation tower at 300 ^° C or more and 350 ^° C or less, the second light oil having a boiling point lower than that of naphthalene; A second distillation step of separating the mixed oil comprising naphthalene, a wash oil, and a modified tar; and a modified tar; and a mixed oil of the result of the second distillation step. Oi l) distillation at 220 ^° C or more and 260 ^° C or less in the third distillation tower, three distillation step of separating the naphthalene, absorbent oil, and the reforming tar, respectively; reforming tar production process to provide.

Here, (boiling point of 180 t to naphthalene) means any one of the boiling point of 180 ^° C to naphthalene, and A to B means A or more and B or less, unless otherwise defined.

1 is an exemplary schematic diagram of an apparatus that may be used in the modified tar production process of one embodiment of the present invention. Thus, such a device can be modified in various forms. Hereinafter, with reference to Figure 1, the modified tar production process of an embodiment of the present invention will be described.

Tar, a by-product of the coke oven, is maintained at a temperature above 70 ^° C and below 100 ^° C to prevent solidification in storage tanks (not shown). Afterwards, the storage tank is connected to the first distillation tower 101 through a pipe, and in the middle of the pipe through a heat exchanger or a heater (not shown) to a temperature of 110 ^° C or more and 180 ^° C to a temperature lower than the boiling point of naphthalene. It is heated up. The heated tar is distilled from the first distillation tower, specifically, water exits to the top in the form of steam, and the remaining tar falls to the bottom except for water. As a result, the temperature of the tar in the first heater 104 may be easily increased in a subsequent step. At this time, the boiling point (180 ^° C Below the boiling point of naphthalene) may also be evaporated to exit the top of the first distillation tower in gaseous state. Thus, the water coming out to the top and the boiling point (180 ^° C ~ boiling point of naphthalene) is separated in a mixed state in a water separator 106 is provided with a separate first light oil (light oil). Thereafter, water and the first light oil may be separated through the water separator 106, and only the first light oil may be separated into a separate first light oil storage tank 107. The first light oil thus separated may be used as fuel in the coke manufacturing process or the reforming tar process, or may be sold separately. After removing the water and the first light oil removed from the U distillation tower to the bottom, the tar is heated to a temperature of 300 ^° C. or more and 35 CTC or less through a separately equipped crab 1 heater 104, and then the second distillation tower (102 Is transferred to). The distillation temperature of the second distillation step is limited as described above because it is easy to separate the absorbent oil in the above range, and when it exceeds 350 ^° C., unnecessary energy is supplied, which is disadvantageous in energy loss. In the second distillation tower, the second, consisting of components lower than naphthalene (about 218 ^° C) by boiling point _. Light oil; Naphthalene, absorbent oil, and mixed tar mixed with modified tar; and modified tar. Here, the absorbent oil is a material composed of a component higher than naphthalene on the basis of the break point, and is a liquid in the form of a complex having a boiling point generally in the range of about 230 ^° C. to 330 ^° C. At this time, the crab distillation tower 102 may be operated at atmospheric pressure, and the steam is injected through the steam pipe 111 to increase the efficiency of separation. By injecting the steam, and the second ^"to increase the flow rate of the internal distillation tower 102, the separation efficiency can be improved. The second light oil from the second distillation tower 102 can be transferred to the water separator 106 and mixed with the water vapor, crab 1 light oil from the first distillation tower. Thereafter, water and light oils may be separated through the water separator 106 as described above, and the separated light oil may be used as fuel in a coke manufacturing process or a modified tar process or sold separately. In addition, of course, the second light oil separated from the second distillation tower 102 may further include water vapor remaining. The mixed oil separated in the second distillation tower 102 is transferred to the crab 3 distillation tower 103 without additional heating, and is operated at a temperature of 220 ^° C. or higher and 260 ^° C. or lower in the third distillation tower 103. Distilled). Accordingly, naphthalene is separated from the upper end of the third distillation tower 103 and stored in the naphthalene storage tank 108 in a liquid state. In the middle portion of the Crab 3 distillation tower 103, the absorbent oil is separated and stored in the absorbent oil storage tank 109 to be used in the Hwaseong plant. At the bottom of the third distillation tower 103, the modified tar is separated and transferred to the modified tar storage tank 110 and stored. By performing the third distillation step in the above temperature range, distillation of naphthalene is possible, and the absorbent oil can be separated at a level of about 4%. After the third distillation step in the crab 3 distillation tower (103), after the reforming tar (Tar) separated in the third distillation step through the second heater (105), the third May be reintroduced into distillation tower 103. Thus, by further distilling the separated modified tar in the third distillation tower 103, the purity of the modified tar can be further improved.

In addition, the modified tar coming from the bottom of the second distillation tower 102 and / or the bottom of the crab 3 distillation tower 103 may be recycled to the second distillation tower 102 through a separate circulation pipe 112. . Specifically, before being heated by the first heater 104 described above, after the separated water and / or the first light oil at the bottom of the first distillation tower 101 are mixed with the removed product, the first heater ( And heated to 104 to a distillation tower 102. Thus, the recycled reforming tar may be performed by repeating the distillation process in the second distillation tower 102 and the third distillation tower 103, thereby improving the purity. The modified tar finally obtained through the above-described process can be used to increase the strength by mixing with the coal for coke as caking complement in the coke production process. In addition, the odor caused by the existing unmodified tar can be removed, the blockage of the pipes by naphthalene can be eliminated, and the strength of the coke coal can be improved while improving the side effects of the existing additives. In addition, by-products of modified tar production processes, such as light oil, naphthalene and absorbent oil, can be sold separately, resulting in additional imports. Although the present invention has been described above, it will be readily understood by those skilled in the art that various modifications and variations are possible without departing from the spirit and scope of the claims set out below.

[Explanation of code]

101 Crab 1 Distillation Tower 102 Hang 12 Distillation Tower

103 third distillation tower 104 first heater

105 Second Heater 106 Water Separator

107 light oil storage tank 108 naphthalene storage tank

109 absorbent oil storage tank 110 modified tar storage tank

111 Steam Line 112 Circulation Line

Claims

[Claims]

[Claim 1]

Tar, a by-product of the coke process, is distilled in the first distillation tower above 100 ^° C (180 ^° C ~ boiling point of naphthalene), water and / or boiling point (180 ^° C ~ boiling point of naphthalene) below 1 distillation step to remove the first Light Oil,

Distilling the resultant from which water and / or the first light oil was removed in the first distillation step at 30CTC or more and 350 ^° C or less in a 12 distillation tower, the boiling point of which is lower than naphthalene; A second distillation step of separating the mixed oil (Mixed Oil); and the modified Tar; each containing naphthalene, absorbent oil, and modified Tar, and

A third distillation step of distilling mixed oil (Mixed Oil) from the result of the second distillation step ^{at a} temperature of 220 ^° C. or more and 26 CTC or less in a third distillation tower to separate naphthalene, absorbent oil, and modified Tar, respectively. doing,

Modified tar production process.

[Claim 2]

In paragraph 1,

In the second distillation step,

In the first distillation step, the product from which water and / or the first light oil is removed is heated to 300 ^° C. or more and 350 ton or less and transferred to the second distillation tower.

Modified tar production process.

[Claim 3]

In paragraph 2,

In the third distillation step,

Mixed oil (Mixed Oi l) of the result of the two distillation step is transferred to the third distillation tower without additional heating,

Modified Tar Production Process.

[Claim 4]

In paragraph 3, And reforming tar separated in the second distillation tower and / or the third distillation tower to recycle the second tar to the second distillation tower.

[Claim 5]

In paragraph 1,

In the second distillation step, to supply steam to the second distillation tower,

Modified tar production process.

[Claim 6]

In paragraph 1,

After the three distillation stages,

After reboiling the modified tar (Tar) separated in the three distillation step through a heater (heater), and further comprising the step of re-introducing the third distillation tower,

Modified Tar Production Process.

[Claim 7]

In paragraph 4,

In the second distillation step,

The water and / or crab 1 light oil separated in the first distillation step are removed, and the modified tar separated from the recycled second distillation tower and / or the third distillation tower is It is heated to 300 ^° C or more and 350 ^° C or less to be introduced into the second distillation tower ，

Modified tar production process.

[Claim 8]

In paragraph 1,

Before the first distillation step,

The method further includes the step of heating tar, a by-product of the coke process, through a heat exchanger or a heater to be introduced into a crab distillation tower.

Modified tar production process. ᅳ [Claim 9]

In paragraph 1,

The modified tar is

Modified tar production process, which is intended for caking additives to be added to the coke manufacturing process.