KR20080056937A - Naphthalene recovery method in ammonium lequor generated in coke making process - Google Patents

Naphthalene recovery method in ammonium lequor generated in coke making process Download PDF

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KR20080056937A
KR20080056937A KR1020060130150A KR20060130150A KR20080056937A KR 20080056937 A KR20080056937 A KR 20080056937A KR 1020060130150 A KR1020060130150 A KR 1020060130150A KR 20060130150 A KR20060130150 A KR 20060130150A KR 20080056937 A KR20080056937 A KR 20080056937A
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solvent
naphthalene
ordination
hexane
normal
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KR101268125B1 (en
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이현
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재단법인 포항산업과학연구원
주식회사 포스코
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0004—Crystallisation cooling by heat exchange
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B43/00—Preventing or removing incrustations
    • C10B43/02—Removing incrustations
    • C10B43/08—Removing incrustations with liquids

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  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

A method for recovering naphthalene contained in ammonium liquor is provided to prevent closing of a supply pipe due to the organic component and naphthalene and breakdown of facilities due to closing of the supply pipe by efficiently recovering an organic component and naphthalene contained in ammonia liquor. A method for recovering naphthalene contained in ammonium liquor generated in the coke manufacturing process comprises: a solvent extracting step(A) mixing ammonia liquor with light oil, normal-hexane, or a mixture of the light oil and the normal-hexane, thereby dissolving an organic component contained in ammonia liquor into a solvent to extract the organic component by the solvent; a distilling step(B) of distilling the organic component extracted by the solvent; a crystallizing step(C) of crystallizing the residues by cooling residues that have not been distilled but have been remained in the distilling step; and a filtering and recovering step(D) of recovering naphthalene by filtering a crystal produced in the crystallizing step. Further, the distilling step is performed at a temperature ranged from 60 °C to 100 °C.

Description

안수 중에 함유된 나프탈렌의 회수방법{Naphthalene recovery method in ammonium lequor generated in coke making process}Naphthalene recovery method in ammonium lequor generated in coke making process

도 1은 일반적인 코크오븐가스 정제장치의 개략도 1 is a schematic view of a typical coke oven gas purification device

도 2는 본 발명의 일실시예에 따른 안수 중에 함유된 나프탈렌의 회수방법의 흐름도2 is a flowchart of a method for recovering naphthalene contained in ordination according to an embodiment of the present invention.

도 3은 도 2의 바람직한 용매의 함유량을 나타내는 그래프3 is a graph showing the content of the preferred solvent of FIG.

도 4는 도 3의 바람직한 증류온도를 나타내는 그래프4 is a graph showing the preferred distillation temperature of FIG.

<도면의 주요부분에 대한 부호의 설명><Description of the symbols for the main parts of the drawings>

100 : 코크오븐가스 정제장치 10 : 흡수탑 100: coke oven gas purification device 10: absorption tower

11 : 안수 공급배관 20 : 코크오븐가스 공급라인 11: water supply pipe 20: coke oven gas supply line

30 : 코크오븐가스 배출라인 40 : 불용성탄산칼슘 필터30 coke oven gas discharge line 40 insoluble calcium carbonate filter

A : 용매추출단계 B : 증류단계A: solvent extraction step B: distillation step

C : 결정화단계 D : 여과회수단계C: crystallization step D: filtration recovery step

본 발명은 코크스 제조공정에서 발생되는 안수 중에 함유된 나프탈렌의 회수 방법에 관한 것으로서, 보다 상세하게는 안수 중에 함유된 유기성분 및 나프탈렌을 효율적으로 회수함으로서, 상기 유기성분 및 나프탈렌에 의한 공급배관의 폐쇄 및 그로인한 설비의 고장을 방지할 수 있도록 한 안수 중에 함유된 나프탈렌의 회수방법에 관한 것이다.The present invention relates to a method for recovering naphthalene contained in the ordination generated in the coke manufacturing process, and more particularly, by efficiently recovering the organic component and naphthalene contained in the ordination, thereby closing the supply pipe by the organic component and naphthalene. And it relates to a method for recovering naphthalene contained in the ordination so as to prevent the failure of the equipment thereby.

일반적으로 석탄을 이용한 건류 공정을 통한 코크스 제조과정에서는 코크오븐가스, 타르 및 수분이 발생되는데, 이러한 생성물 중 타르 및 수분은 액상상태로 회수 처리되며, 가스 상태인 코크오븐가스는 포집되어 제철소내의 에너지원으로 사용된다. Generally, coke oven gas, tar, and water are generated in the coke manufacturing process through the coal-drying process using coal. Among these products, tar and water are recovered and processed in a liquid state, and the gaseous coke oven gas is collected and energy in the steel mill. Used as a circle.

그러나, 상기 코크오븐가스 중에는 연료로 활용되지 못하는 이산화탄소, 이산화황 및 유입 산소가 일부 함유되어 있어 코크오븐가스의 부피증가와 함께 발열량을 감소시키게 되며, 대기중으로 방출되어 이산화황에 의한 대기오염 및 이산화탄소에 의한 지구 온난화 현상 등을 야기시키는 원인이 되고, 상기와 같은 문제점을 해결하기 위하여 코크오븐가스는 정제공정을 거치게 된다.However, the coke oven gas contains some carbon dioxide, sulfur dioxide and inflowing oxygen, which are not used as fuels, thereby reducing the calorific value with the increase of the volume of the coke oven gas, and being released into the atmosphere, caused by air pollution and carbon dioxide caused by sulfur dioxide. Coke oven gas is subjected to a purification process in order to cause global warming, and to solve the above problems.

도 1은 코크오븐가스에 함유된 산화가스를 제거하기 위한 일반적인 코크오븐가스 정제장치의 개략도로서, 이를 통해 코크오븐가스의 정제공정을 살펴보면, 코크스의 제조과정에서 생성된 코크오븐가스는 코크오븐가스 정제장치(100)의 코크오븐가스 공급라인(20)을 통해 장치 내부로 삽입되어 장치 상부에 구성된 흡수탑(10)을 통과하여 정제된 후 코크오븐가스 배출라인을 통해 배출되게 된다.1 is a schematic view of a general coke oven gas refining apparatus for removing oxidized gas contained in the coke oven gas, when looking at the process for refining the coke oven gas, the coke oven gas generated in the manufacturing process of the coke is coke oven gas It is inserted into the apparatus through the coke oven gas supply line 20 of the refining apparatus 100 is purified through the absorption tower 10 configured in the upper portion of the apparatus is discharged through the coke oven gas discharge line.

상기의 흡수탑(10)에는 코크오븐가스에서 산화가스를 흡수하여 제거하기 위한 안수(암모니아수)가 안수 공급배관(11)을 통해 공급되어 분사되며, 분사 후의 흡수액은 코크오븐가스의 이산화탄소와의 반응에 의해 생성된 불용성탄산칼슘을 포함하고 있어, 외부에 별도로 구성된 불용성탄산칼슘필터(40)를 거쳐 순환되면서 불용성탄산칼슘을 제거하고 다시 재활용되어 흡수탑(10)에서 분사되게 된다.In the absorption tower 10, the ordination (ammonia water) for absorbing and removing the oxidizing gas from the coke oven gas is supplied through the ordination supply pipe 11 and injected, and the absorbing liquid after the injection is reacted with the carbon dioxide of the coke oven gas. Including the insoluble calcium carbonate produced by, by circulating through the insoluble calcium carbonate filter 40 configured separately in the outside to remove the insoluble calcium carbonate is recycled and is sprayed again in the absorption tower (10).

그러나 상기 안수에는 나프탈렌을 포함하는 유기성분이 함유되어 있어, 상기 안수 공급배관(11)을 통한 공급 시, 상기 유기성분 및 나프탈렌이 공급배관(11)에 고착되어 공급배관(11)을 폐쇄시키게 되고 공급배관(11)의 폐쇄로 인해 설비의 정상적인 운전이 방해되어 설비 전체가 고장을 일으키는 등의 문제점이 있었다.However, the ordination contains an organic component including naphthalene, so that the organic component and naphthalene are fixed to the supply pipe 11 to close the supply pipe 11 when supplied through the ordination supply pipe 11. Due to the closing of the pipe 11, there is a problem such that the normal operation of the equipment is disturbed and the entire equipment is broken.

안수에 용매를 혼합하여 유기성분을 용매추출하고 추출된 유기성분을 증류시켜 나프탈렌의 회수함으로서, 상기 유기성분 및 나프탈렌에 의한 공급배관의 폐쇄 및 그로인한 설비의 고장을 방지할 수 있도록 하는 안수 중에 함유된 나프탈렌의 회수방법을 제공함에 목적이 있다.By mixing the solvent in the ordination, the organic component is solvent-extracted and the extracted organic component is distilled to recover naphthalene, which is contained in the ordination so as to prevent the closing of the supply pipe by the organic component and naphthalene and thereby the failure of the equipment. It is an object of the present invention to provide a method for recovering naphthalene.

상술한 목적을 달성하기 위한 본 발명의 특징은, 안수에 경유 또는 노말-헥산 또는 경유와 노말-헥산의 혼합물을 혼합하여 안수에 포함된 유기성분을 용해시킴으로서 용매추출하는 용매추출단계(A)와, 상기 용매에 의해 추출된 유기성분을 증류시키는 증류단계(B)와, 상기 증류단계에서 증류되지 않고 잔유된 잔유물을 냉각하여 결정화시키는 결정화단계(C)와, 상기 결정화단계에서 생성된 결정을 여과하여 나프탈렌을 회수하는 여과회수단계(D)를 포함하는 안수 중에 함유된 나프탈렌의 회수방법이다.A feature of the present invention for achieving the above object is a solvent extraction step (A) and solvent extraction by dissolving the organic components contained in the ordination by mixing light oil or normal-hexane or a mixture of light oil and normal-hexane in the ordination; A distillation step (B) of distilling the organic components extracted by the solvent, a crystallization step (C) of cooling and crystallizing the residues remaining without distillation in the distillation step, and filtering the crystals produced in the crystallization step It is a method of recovering naphthalene contained in the ordination, including the filtration recovery step (D) for recovering naphthalene.

상기 본 발명의 특징에 의한 용매추출단계(A)는, 용매로서 사용되는 경유 또는 노말-헥산 또는 경유와 노말-헥산의 혼합물이 안수에 5 부피% 이상 함유되게 하는 실시예를 구성할 수 있다.Solvent extraction step (A) according to the characteristics of the present invention, it is possible to constitute an embodiment in which light oil or normal-hexane or a mixture of light oil and normal-hexane to be contained in the ordinal 5% by volume or more used as a solvent.

또한, 상기 본 발명의 특징에 의한 증류단계(B)는, 증류온도가 60℃ 이상인 상태에서 실시하는 실시예를 구성할 수 있다.In addition, the distillation step (B) according to the characteristics of the present invention, it is possible to constitute an embodiment carried out in a state where the distillation temperature is 60 ℃ or more.

또한, 경유와 노말-헥산의 혼합물은, 경유와 노말-헥산이 1 : 1로 혼합하여 사용하는 실시예를 구성할 수 있다.In addition, the mixture of light oil and normal-hexane can comprise the Example which mixes and uses light oil and normal-hexane 1: 1.

상기 본 발명의 목적과 특징 및 장점은 첨부도면 및 다음의 상세한 설명을 참조함으로서 더욱 쉽게 이해될 수 있을 것이다.The objects, features and advantages of the present invention will be more readily understood by reference to the accompanying drawings and the following detailed description.

이하, 첨부된 도면을 참조하여 본 발명의 바람직한 실시예의 구성 및 그 작용 효과에 대해 상세히 설명하면 다음과 같다.Hereinafter, with reference to the accompanying drawings will be described in detail the configuration and effect of the preferred embodiment of the present invention.

도 2는 본 발명의 일실시예에 따른 안수 중에 함유된 나프탈렌의 회수방법의 흐름도로서, 본 발명의 안수 중에 함유된 나프탈렌의 회수방법은 용매추출단계(A)와, 증류단계(B)와, 결정화단계(C)와, 여과회수단계(D)를 포함하여 구성된다.Figure 2 is a flow chart of the recovery method of naphthalene contained in the ordination according to an embodiment of the present invention, the recovery method of naphthalene contained in the ordination of the present invention is a solvent extraction step (A), distillation step (B), And a crystallization step (C) and a filtration recovery step (D).

상기 용매추출단계(A)는, 안수에 용매를 혼합하여 안수에 포함된 나프탈렌을 포함하는 유기성분을 용해시킴으로서 용매추출하는 단계로서, 안수 중에 함유된 유기성분보다 높은 용해도를 가지는 용매를 이용하여 상기 나프탈렌을 포함하는 유기성분을 용매에 용해시켜 추출하는 것으로, 상기 용매로서 경유 또는 노말-헥산 또는 경유와 노말-헥산의 혼합물을 안수에 5 부피% 이상 혼합하는 것이 바람직하며, 그 이유는 후술되어질 실험예 1을 통해 증명하였다.The solvent extraction step (A) is a step of solvent extraction by dissolving an organic component including naphthalene contained in the ordination by mixing a solvent in the ordination, using a solvent having a higher solubility than the organic component contained in the ordination The organic component containing naphthalene is extracted by dissolving it in a solvent. It is preferable to mix light oil or normal-hexane or a mixture of light oil and normal-hexane as 5% or more by volume in ordination, and the reason for this will be described later. Example 1 demonstrates.

또한, 상기 경유 또는 노말-헥산의 단독 사용 외에 경유와 노말-헥산을 혼합하여 사용할 경우, 경유와 노말-헥산을 1 : 1로 혼합하는 것이 가장 바람직하며, 상기 경유의 단독 사용, 노말-헥산의 단독 사용, 경유와 노말-헥산의 혼합물의 사용에 따른 유기성분의 추출량에는 큰 차이가 없으며, 그 또한 후술되어질 실험예 1을 통해 증명하였다.In addition, when using light oil or normal-hexane in addition to the use of light oil or normal-hexane alone, it is most preferable to mix the light oil and normal-hexane to 1: 1, the use of the light oil alone, of normal-hexane There is no significant difference in the extraction amount of the organic components according to the sole use, the mixture of light oil and normal-hexane, it was also proved through Experimental Example 1 to be described later.

상기 증류단계(B)는, 상기 용매에 의해 추출된 유기성분을 증류시키는 단계로서, 증류온도가 60℃ 이상인 상태에서 물의 비등점인 100℃이하에서 실시하는 것이 가장 바람직하며, 그 이유는 후술되어질 실험예 2를 통해 증명하였다. The distillation step (B) is a step of distilling the organic component extracted by the solvent, it is most preferably carried out at 100 ℃ or less boiling point of water in the state that the distillation temperature is 60 ℃ or more, the reason for which will be described later Proved through example 2.

상기 결정화단계(C)는, 상기 증류단계에서 증류되지 않고 잔유된 잔유물을 냉각하여 결정화시키는 단계이며, 상기 여과회수단계(D)는, 상기 결정화단계에서 생성된 결정을 여과하여 나프탈렌을 회수하는 단계로서, 본 발명은 상기의 각 단계를 거쳐 안수 중에 함유된 나프탈렌을 회수하게 된다.The crystallization step (C) is a step of crystallization by cooling the residues remaining in the distillation step without distillation, and the filtration recovery step (D) is a step of recovering naphthalene by filtering the crystals produced in the crystallization step As the present invention, the naphthalene contained in the ordination is recovered through each of the above steps.

이하, 실험예 1 및 실험예 2를 통하여 상기 용매추출단계(A)에서의 바람직한 용매혼합량 및 증류단계(B)에서의 바람직한 증류온도조건을 산출하면 다음과 같다. Hereinafter, the preferred solvent mixture in the solvent extraction step (A) and the preferred distillation temperature conditions in the distillation step (B) through Experimental Example 1 and Experimental Example 2 are as follows.

실험예 1 용매추출단계(A)에서의 바람직한 용매혼합량 산출Experimental Example 1 Calculation of the preferred amount of solvent mixture in the solvent extraction step (A)

본 발명은 코크스 제조과정에서 발생하는 안수중에 함유된 유기성분을 효율적으로 회수하기 위해서 물리화학적인 방법인 용매에 용해시켜 추출 분리하도록 하며, 사용하는 용매는 여러가지의 종류를 사용할 수 있지만 본 발명에서는 공정에서 회수된 경유와 노말헥산을 사용하여 시험을 실시하였고, 이에 따른 조건을 설정하였다. 상기 용매의 사용량은 공정시간을 포함하여 확정하였는데 경유와 노말-헥산 을 각각 또는 혼합하고 안수에 함유하여 추출되는 양을 실험한 것이다. The present invention is to dissolve and extract by dissolving in a solvent, which is a physicochemical method in order to efficiently recover the organic components contained in the ordination generated during the coke manufacturing process, in the present invention can be used in various kinds of process The test was carried out using diesel and normal hexane recovered from, and the conditions were set accordingly. The amount of the solvent used was determined including the process time, and the amount of the solvent extracted and mixed with light oil and normal-hexane, respectively, was measured.

본 실험예에서는 안수중에 함유된 유기성분을 용매추출함에 있어, 용매추출단계(A)에서의 바람직한 용매혼합량을 부피%로 결정하기 위한 실험예로 용매추출을 위해서 충분한 시간을 혼합하였으며, 추출 시간을 동시에 시험한 결과이다. 따라서 본 발명의 공정에서는 충분한 혼합용매추출을 위해서 10분간, 상온 25℃을 기준으로 실시하였으며, 그 결과 용매의 혼합량(부피%)에 따른 추출되는 양(%)를 정리하여 도 3에 나타내었다.In this Experimental Example, in extracting the organic components contained in the ordinal solvent, an experimental example for determining the volume of the preferred solvent mixture in the solvent extraction step (A) by volume% was mixed a sufficient time for solvent extraction, extraction time Simultaneous test results. Therefore, in the process of the present invention was carried out based on 25 ℃ at room temperature for 10 minutes in order to extract a sufficient mixed solvent, as a result it is shown in Figure 3 summarized the amount (%) to be extracted according to the mixing amount (vol%) of the solvent.

도 3에 도시된 바와 같이, 안수 중에 함유된 유기성분을 추출하는데 용매를 사용하는 양은 5 부피%이상을 함유시켜야 95% 이상의 추출이 가능하며, 용매로 각각 경유 또는 노말-헥산을 사용하거나 혼합하여 사용하여도 큰 차이가 없음을 알 수 있으며, 용매혼합량은 용매를 안수에 5부피%이상 혼합시켜 추출하는 것이 본 발명의 바람직한 조건이 된다. 상한 값으로는 일반적으로 사용하는 10 부피%이하에서 실시하는 것이 바람직하다. As shown in Figure 3, the amount of the solvent used to extract the organic components contained in the ordination should be contained at least 5% by volume or more can be extracted more than 95%, using light oil or normal-hexane as a solvent or mixed It can be seen that there is no significant difference even if used, the solvent mixture amount is preferably extracted by mixing the solvent in ordinal 5% by volume or more. As an upper limit, it is preferable to carry out at 10 volume% or less normally used.

실험예 2 증류단계(B)에서의 바람직한 증류온도조건 산출Experimental Example 2 Calculation of the preferred distillation temperature conditions in the distillation step (B)

본 실험예에서는 용매에 의해서 추출된 유기성분을 분리하는데 증류방법을 사용하게 되며, 나프탈렌을 회수하기 위해서 일부 기화성이 강한 용매을 일차적으로 증류하고, 상기 증류과정에서 나프탈렌은 잔유물에 포함되도록 하기 위한 증류온도조건 설정이 필요함에따라 증류온도와 나프탈렌 함유량 및 용매회수량과 관련하여 실험하였으며, 통상 공정시간이 20분간 진행됨으로 증류시간 20분을 기준으로 용매 회수율을 산정하였고 그 결과를 도 4에 나타내었다. In the present experimental example, a distillation method is used to separate the organic components extracted by the solvent. In order to recover naphthalene, some of the highly vaporizable solvents are first distilled, and in the distillation process, naphthalene is included in the residue. Experiments were made regarding the distillation temperature, naphthalene content, and solvent recovery amount as the condition setting was required. As a result, the solvent recovery rate was calculated based on the distillation time of 20 minutes since the process time was 20 minutes, and the results are shown in FIG. 4.

도 4에 도시된 바와 같이, 용매의 증류 회수율이 90%이상 되는 온도조건은 60℃이상이며, 60℃미만에서는 회수율이 매우 감소한 현상을 보인다. 따라서 본 발명에서는 증류온도가 60℃이상에서 실시하는 것이 증류회수율을 높일 수 있는 바람직한 조건이 되며, 증류공정은 고압의 스팀을 사용하게 되는데 열전달 상태를 감안하면 물의 비증점인 100℃이하의 조건이 바람직하다. As shown in FIG. 4, the temperature condition under which the distillation recovery rate of the solvent is 90% or more is 60 ° C. or higher, and when the temperature is lower than 60 ° C., the recovery rate is very decreased. Therefore, in the present invention, the distillation temperature is performed at 60 ° C. or higher, which is a preferable condition for increasing the distillation recovery rate. The distillation process uses high pressure steam. desirable.

본 발명은 상기 실험예를 통해 산출된 각 조건에 따라서 용매추출단계(A)와, 증류단계(B)를 진행시킨 후에 용매가 증류 분리된 잔유물을 냉각과정을 거쳐 결정화하고 여과하여 나프탈렌을 효율적으로 회수함으로서, 상기 유기성분 및 나프탈렌에 의한 공급배관의 폐쇄 및 그로인한 설비의 고장을 방지할 수 있게 된다.According to the present invention, the solvent extraction step (A) and the distillation step (B) are carried out according to the conditions calculated through the above experimental example, and the residues from which the solvent is distilled off are cooled and crystallized and filtered to efficiently naphthalene. By recovering, it is possible to prevent the closing of the supply pipe by the organic component and naphthalene and the failure of the equipment.

이외에도 본 발명인 안수 중에 함유된 나프탈렌의 회수방법은 다양하게 변형실시될 수 있는 것으로, 본 발명의 목적범위를 일탈하지 않는 한, 변형되는 실시예들은 모두 본 발명의 권리범위에 포함되어 해석되어야 한다.In addition, the recovery method of naphthalene contained in the ordination of the present invention may be variously modified, and the embodiments to be modified should be construed as being included in the scope of the present invention, without departing from the scope of the present invention.

이상의 본 발명에 의하면, 안수 중에 함유된 유기성분 및 나프탈렌을 효율적으로 회수함으로서, 상기 유기성분 및 나프탈렌에 의한 공급배관의 폐쇄 및 그로인한 설비의 고장을 방지할 수 있게 되는 등의 이점을 얻을 수 있게 된다.According to the present invention, by efficiently recovering the organic components and naphthalene contained in the ordination, it is possible to obtain advantages such as the closing of the supply pipe by the organic components and naphthalene and the failure of the equipment thereby do.

Claims (4)

코크스 제조공정에서 발생되는 안수 중에 함유된 나프탈렌의 회수방법에 있어서, In the recovery method of naphthalene contained in the ordination generated in the coke manufacturing process, 안수에 경유 또는 노말-헥산 또는 경유와 노말-헥산의 혼합물을 혼합하여 안수에 포함된 유기성분을 용해시킴으로서 용매추출하는 용매추출단계(A)와,A solvent extraction step (A) of extracting a solvent by dissolving organic components included in ordination by mixing light oil or normal-hexane or a mixture of light oil and normal-hexane in ordination; 상기 용매에 의해 추출된 유기성분을 증류시키는 증류단계(B)와,A distillation step (B) of distilling the organic component extracted by the solvent, 상기 증류단계에서 증류되지 않고 잔유된 잔유물을 냉각하여 결정화시키는 결정화단계(C)와,A crystallization step (C) of cooling and crystallizing the residue remaining in the distillation step without distillation; 상기 결정화단계에서 생성된 결정을 여과하여 나프탈렌을 회수하는 여과회수단계(D)를 포함하는 것을 특징으로 하는 안수 중에 함유된 나프탈렌의 회수방법.The method for recovering naphthalene contained in the ordination, characterized in that it comprises a filtration recovery step (D) for recovering naphthalene by filtering the crystals produced in the crystallization step. 제 1항에 있어서,The method of claim 1, 용매추출단계(A)는,Solvent extraction step (A), 용매로서 사용되는 경유 또는 노말-헥산 또는 경유와 노말-헥산의 혼합물이 안수에 5 부피% ~ 10부피% 함유되는 것을 특징으로 하는 안수 중에 함유된 나프탈렌의 회수방법.A method for recovering naphthalene contained in ordination, characterized in that 5% by volume to 10% by volume of light oil or normal-hexane or a mixture of light oil and normal-hexane is used as a solvent. 제 1항에 있어서,The method of claim 1, 증류단계(B)는,Distillation step (B), 증류온도가 60℃ 이상에서 물의 비등점인 100℃이하에서 실시하는 것을 특징으로 하는 안수 중에 함유된 나프탈렌의 회수방법.A method for recovering naphthalene contained in ordination, which is carried out at a distillation temperature of 60 ° C. or higher and 100 ° C. or lower, which is the boiling point of water. 제 1항에 있어서,The method of claim 1, 경유와 노말-헥산의 혼합물은,The mixture of light oil and normal-hexane is 경유와 노말-헥산이 1 : 1로 혼합된 것을 특징으로 하는 안수 중에 함유된 나프탈렌의 회수방법.A method for recovering naphthalene contained in ordination, characterized in that light oil and normal-hexane are mixed 1: 1.
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