KR20120067400A - A method for preparing 1,2-dichloroethane - Google Patents
A method for preparing 1,2-dichloroethane Download PDFInfo
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- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims description 30
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 52
- 239000000460 chlorine Substances 0.000 claims abstract description 52
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 51
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000005977 Ethylene Substances 0.000 claims abstract description 34
- 238000006243 chemical reaction Methods 0.000 claims abstract description 25
- 239000006227 byproduct Substances 0.000 claims abstract description 18
- 238000004519 manufacturing process Methods 0.000 claims abstract description 17
- 238000002347 injection Methods 0.000 claims abstract description 10
- 239000007924 injection Substances 0.000 claims abstract description 10
- 239000002904 solvent Substances 0.000 claims description 13
- 239000003054 catalyst Substances 0.000 claims description 10
- UBOXGVDOUJQMTN-UHFFFAOYSA-N 1,1,2-trichloroethane Chemical compound ClCC(Cl)Cl UBOXGVDOUJQMTN-UHFFFAOYSA-N 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 125000001309 chloro group Chemical group Cl* 0.000 claims 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 5
- 229910000041 hydrogen chloride Inorganic materials 0.000 abstract description 5
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 abstract description 5
- 238000005660 chlorination reaction Methods 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- QPFMBZIOSGYJDE-UHFFFAOYSA-N 1,1,2,2-tetrachloroethane Chemical compound ClC(Cl)C(Cl)Cl QPFMBZIOSGYJDE-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- UOCLXMDMGBRAIB-UHFFFAOYSA-N 1,1,1-trichloroethane Chemical compound CC(Cl)(Cl)Cl UOCLXMDMGBRAIB-UHFFFAOYSA-N 0.000 description 1
- 241000283707 Capra Species 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000007810 chemical reaction solvent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/013—Preparation of halogenated hydrocarbons by addition of halogens
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated hydrocarbons
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C19/00—Acyclic saturated compounds containing halogen atoms
- C07C19/01—Acyclic saturated compounds containing halogen atoms containing chlorine
- C07C19/043—Chloroethanes
- C07C19/045—Dichloroethanes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
본 발명은 에틸렌과 염소의 반응에 의해 1,2-디클로로에탄 (EDC)을 제조하는 방법에 관한 것으로, 에틸렌과 염소를 반응기 하부에 별도로 공급하되 염소를 분리 주입한 다음 용해도를 감안하여 효율적으로 반응시켜 1,2-디클로로에탄을 생성시키는 방법을 제공한다.
본 발명에 따르면, 에틸렌에 비해 염소의 용해도가 높은 점을 감안하여 염소를 각기 다른 높이의 분리 주입 장치를 통해 에틸렌보다 상부위치에 공급함으로써 부산물을 효과적으로 억제하고 1,2-디클로로에탄의 선택도를 향상시키며 효율적으로 합성할 수 있다. 또한 적절한 압력강하와 더불어 반응기 전체를 효율적으로 활용함으로써 추가 반응기를 설치하지 않고도 생산량을 증가시킬 수 있고 미반응 염화수소를 줄여 반응기 수명도 연장할 수 있다.The present invention relates to a method for producing 1,2-dichloroethane (EDC) by the reaction of ethylene and chlorine, the ethylene and chlorine are separately supplied to the lower portion of the reactor, but the chlorine is separated and injected to efficiently react in consideration of solubility To provide 1,2-dichloroethane.
According to the present invention, in view of the higher solubility of chlorine than ethylene, by supplying chlorine to an upper position than ethylene through a separate injection device of different heights to effectively suppress the by-products and improve the selectivity of 1,2-dichloroethane It can be synthesized efficiently and efficiently. In addition, with the proper pressure drop, the entire reactor can be efficiently utilized to increase production without installing additional reactors and to extend reactor life by reducing unreacted hydrogen chloride.
Description
본 발명은 에틸렌과 염소의 반응에 의해 1,2-디클로로에탄 (EDC)을 제조하는 방법에 관한 것으로, 에틸렌과 염소를 반응기 하부에 별도로 공급하되 염소를 분리 주입한 다음 용해도를 감안하여 효율적으로 반응시켜 1,2-디클로로에탄을 생성시키는 방법에 관한 것이다. The present invention relates to a method for producing 1,2-dichloroethane (EDC) by the reaction of ethylene and chlorine, the ethylene and chlorine are separately supplied to the lower portion of the reactor, but the chlorine is separated and injected to efficiently react in consideration of solubility To produce 1,2-dichloroethane.
일반적으로 1,2-디클로로에탄의 제조방법은 에틸렌과 염소의 반응에 의한 직접 염소화 방법, 과 에틸렌과 염화수소, 산소의 반응에 의한 산화 염소화 방법으로 구분할 수 있다. Generally, 1,2-dichloroethane may be classified into a direct chlorination method by the reaction of ethylene and chlorine, and an oxidative chlorination method by the reaction of ethylene, hydrogen chloride and oxygen.
상기 직접 염소화 방법에 의해 1,2-디클로로에탄을 제조하는 방법은 주로 액체 매질에서 에틸렌과 염소의 반응으로 이루어진다. 이때 반응 탑 형태의 반응기의 하부에서 에틸렌과 염소는 각각 별도로 반응 탑의 하부로부터 공급된다. 이같이 하부로부터 공급된 에틸렌과 염소는 용매에 용해되고 반응하여 1,2-디클로로에탄을 생성시킨다. 이러한 1,2-디클로로에탄의 제조과정에서 각각의 공정 조건은 1,2-디클로로에탄 이외의 부산물을 생성시키는데 중요한 변수가 된다. The process for producing 1,2-dichloroethane by the direct chlorination method consists mainly of the reaction of ethylene and chlorine in a liquid medium. At the bottom of the reactor in the form of a reaction tower, ethylene and chlorine are each fed separately from the bottom of the reaction tower. As such, ethylene and chlorine supplied from the bottom are dissolved in the solvent and react to produce 1,2-dichloroethane. In the process of producing 1,2-dichloroethane, each process condition is an important variable in generating by-products other than 1,2-dichloroethane.
반응 공정 도중 발생하는 여러 중질 부산물들(트리클로로에탄, 테트라클로로에탄 등)은 1,2-디클로로에탄에서 추가적인 염소화 반응이 진행되면서 발생하고, 이러한 물질들은 1,2-디클로로에탄의 선택도를 감소시키게 된다.
Many heavy by-products (trichloroethane, tetrachloroethane, etc.) that occur during the reaction process occur as additional chlorination reactions occur in 1,2-dichloroethane, which reduces the selectivity of 1,2-dichloroethane. Let's go.
특히 상기 반응에서 반응물을 투입하는 방법에 따라 염소와 에틸렌의 용해도 차이로 인해 용매에 용해되어 반응이 일어나지 않고 기체 상에서 반응할 경우에 부산물이 많이 생성될 수 있다.
In particular, depending on the method of adding the reactants in the reaction due to the difference in the solubility of chlorine and ethylene is dissolved in a solvent can be produced a lot of by-products when reacting in the gas phase does not occur.
이에 미국 특허 제4,873,384호에서는 에틸렌의 염소와 비를 조절하는 기술을 개시한 바 있으며, 미국 특허 제 6,235,953호에서는 새로운 촉매를 첨가하는 기술을 개시한 바 있다. 그러나 아직까지 다수의 부산물 생성을 억제하기엔 미흡한 실정이다. Thus, US Patent No. 4,873,384 discloses a technique for controlling the chlorine and the ratio of ethylene, US Patent No. 6,235,953 discloses a technique for adding a new catalyst. However, it is still insufficient to suppress the generation of many by-products.
본 발명자들은 상기와 같은 문제점을 해결하기 위해 연구를 계속하던 중 에틸렌과 염소의 반응에 의해 1,2-디클로로에탄을 제조함에 있어 염소를 분리 주입하면 부산물의 생성을 최소화하고 1,2-디클로로에탄의 선택도를 향상시킬 수 있음을 발견하고 본 발명을 완성하기에 이르렀다.
The inventors of the present invention continue to solve the above problems in the production of 1,2-dichloroethane by the reaction of ethylene and chlorine when injecting chlorine to minimize the formation of by-products and 1,2-dichloroethane It has been found that the selectivity of can be improved and the present invention has been completed.
즉, 본 발명의 목적은 에틸렌과 염소를 반응기 하부에 별도로 공급하되 염소를 분리 주입한 다음 용해도를 감안하여 효율적으로 반응시켜 1,2-디클로로에탄을 생성시키는 방법을 제공하는데 있다. That is, an object of the present invention is to provide ethylene and chlorine separately supplied to the bottom of the reactor, but chlorine is separately injected and then reacted efficiently in consideration of solubility to produce 1,2-dichloroethane.
상기 목적을 달성하기 위하여 본 발명에서는, 1,2-디클로로에탄과 촉매를 포함하는 순환 용매 존재하에 에틸렌과 염소를 반응시켜 1,2-디클로로에탄을 제조하는 방법에 있어서, 상기 염소의 투입 위치를 조절하는 것을 특징으로 하는 1,2-디클로로에탄의 제조방법을 제공한다.
In order to achieve the above object, in the present invention, in the method for producing 1,2-dichloroethane by reacting ethylene and chlorine in the presence of a circulating solvent containing 1,2-dichloroethane and a catalyst, It provides a method for producing 1,2-dichloroethane, which is controlled.
이하, 본 발명에 대하여 상세하게 설명한다. EMBODIMENT OF THE INVENTION Hereinafter, this invention is demonstrated in detail.
본 발명에서는 염소가 에틸렌보다 용해도가 높다는 점에 착안하여, 에틸렌의 상부 위치에 염소를 다단계로 분리 주입함으로써 반응 생산성을 높이고, 미반응 염화수소를 줄이며, 결과적으로 반응기의 수명까지 연장할 수 있는 공정을 제공하는 것을 일 기술적 특징으로 한다.
In view of the fact that chlorine has higher solubility than ethylene, the present invention provides a process for increasing reaction productivity, reducing unreacted hydrogen chloride, and consequently extending the lifetime of the reactor by injecting chlorine in multiple stages in the upper position of ethylene. It is one technical feature to provide.
즉, 도 1에서 보듯이, 종래 방법에서는 반응기 내 동일 위치에서 염소와 에틸렌이 각각 분리되어 투입되나, 본 발명에서는 도 2에 도시한 바와 같이, 염소에 비해 상대적으로 용해도가 낮은 에틸렌이 가장 하부에서 투입되며, 염소는 그 상단부에 위치하게 된다.
That is, as shown in Fig. 1, in the conventional method, chlorine and ethylene are separately introduced into the reactor at the same position, but in the present invention, as shown in Fig. 2, ethylene having a lower solubility than chlorine is at the bottom. And chlorine is placed at its upper end.
이뿐 아니라, 염소의 주입은 다단 분리 주입으로 이루어지는 것이 바람직하다. 즉, 하기 실시 예에서 규명된 바와 같이, 하단부:중간부:상단부의 3단을 통하여 3:1:1의 비로 투입되는 것이 가장 바람직하며, 하단부:중간부의 2단을 통하여 4:1의 비로 투입되는 것도 좋다.
In addition to this, it is preferable that the injection of chlorine consists of a multi-stage separation injection. That is, as it is clear in the following examples, it is most preferably introduced in a ratio of 3: 1: 1 through the three stages of the lower portion: the middle portion: the upper portion, and the ratio is 4: 1 through the two stages of the lower portion: the middle portion. It is good to be.
도 2에서 도시한 반응기 (1)은 에틸렌(6)과 염소(7)가 투입되기 위한 스파져 (8)와 1,2-디클로로에탄과 촉매 포함 순환 용매를 공급하기 위한 루프(5), 그리고 반응으로 생성된 액상 1,2-디클로로에탄 (3)이 발열 반응에 의해 반응기 상부에서 증발하여 기상 1,2-디클로로에탄 (2)으로 배출되는 시스템으로 이루어진다. The
이러한 1,2-디클로로에탄의 제조과정에서 반응온도, 반응기에 반응용매로 사용되는 1,2-디클로로에탄의 순도 및 반응물인 에틸렌과 염소의 투입비율과 같은 각각의 공정조건은 1,2-디클로로에탄 이외의 부산물을 생성시키는데 중요한 변수가 된다.
In the process of producing 1,2-dichloroethane, the respective process conditions such as the reaction temperature, the purity of 1,2-dichloroethane used as the reaction solvent in the reactor, and the input ratio of ethylene and chlorine, the reactants, are 1,2-dichloro. It is an important variable in producing by-products other than ethane.
본 발명은 1,2-디클로로에탄 용매 중에서 에틸렌과 염소의 반응으로부터 1,2-디클로로에탄을 합성하는 방법에 있어, 상기 1,2-디클로로에탄 용매를 순도 85 내지 99.9%로, 상기 에틸렌/염소의 비율은 1.0 내지 1.2로, 그리고 반응온도를 100 내지 125 ℃로 하는 것을 제공한다.
The present invention is a method for synthesizing 1,2-dichloroethane from the reaction of ethylene and chlorine in 1,2-dichloroethane solvent, the 1,2-dichloroethane solvent in a purity of 85 to 99.9%, the ethylene / chlorine Provides a ratio of 1.0 to 1.2 and a reaction temperature of 100 to 125 ° C.
바람직하게는 순환 용매인 1,2-디클로로에탄의 순도가 90 내지 99%에서 부산물의 생성이 적으며 반응 온도는 125 ℃ 이상에서 부산물의 생성이 급격히 증가하게 된다. 특히 110 내지 120 ℃ 범위에서 가장 작게 발생한다. 에틸렌과 염소의 비율은 미반응 염소의 배출을 최소화하기 위해 에틸렌 과다투입 기준으로 1.05:1 내지 1.15:1에서 부산물이 가장 작게 발생한다. 순환 용매에 포함되어 있는 촉매는 반응기 내부에서 자체 생성되거나 반응기 하부에 투입되는 FeCl3이며 촉매 농도는 300 내지 3000 ppm인 것이 바람직하다.
Preferably, the purity of the circulating
상기 발열 반응에 의해 반응기 용매의 온도가 상승하게 되며, 약간 냉각된 1,2-디클로로에탄과 촉매 포함 순환 용매와 함께 증발을 통해 반응열을 회수하게 된다. The temperature of the reactor solvent is increased by the exothermic reaction, and the heat of reaction is recovered through evaporation with the slightly cooled 1,2-dichloroethane and the circulating solvent including the catalyst.
따라서, 본 발명에서와 같은 염소의 분리 주입을 통해 반응열이 국부적으로 높아지는 영역을 제거하여 고온에서 증가하는 중질 부산물(예를 들어, 1,1,2-트리클로로에탄 등)의 형성을 억제할 수 있다.
Therefore, the separation injection of chlorine as in the present invention can eliminate the region where the heat of reaction is locally increased to suppress the formation of heavy by-products (eg, 1,1,2-trichloroethane, etc.) that increase at high temperatures. have.
또한 에틸렌에 비해 용해도가 높은 염소를 각각 다른 높이의 분리 주입 장치로서 스파져 (8)를 통해 공급함으로써 부산물을 효과적으로 억제하고, 1,2-디클로로에탄의 선택도를 향상시키며 효율적으로 합성할 수 있다. 또한, 적절한 압력강하와 반응기 전체를 효율적으로 활용함으로써 추가 반응기의 설치 없이 생산량을 증가시킬 수 있다.
In addition, by supplying chlorine, which has a higher solubility than ethylene, through a sparger (8) as a separate injection device having a different height, the by-products can be effectively suppressed, and the selectivity of 1,2-dichloroethane can be improved and synthesized efficiently. . In addition, by utilizing the appropriate pressure drop and the entire reactor efficiently, production can be increased without installing additional reactors.
한편, 염소 주입 장치인 스파져 (8)는 염소의 용해속도와 반응속도를 고려하여 1 내지 3 m 간격으로 설치가 가능하며 염소압축기의 용량과 스파져 홀에서의 염소 유량의 균일성을 확보하기 위해 적절한 압력강하 및 홀 유속 등을 고려하여 스파져의 개수와 홀 사이즈, 및 개수를 결정할 수 있다. 특히 스파져는 2 내지 3단의 스파져로 이루어지는 것이 바람직하며, 홀 개수는 50 내지 200 개 범위 내이고, 홀 사이즈는 4 내지 10 mm 범위 내인 것이 바람직하다. On the other hand, the
본 발명에 의하면, 에틸렌의 상부 위치에 염소를 다단계로 분리 주입함으로써 반응 생산성을 높이고, 미반응 염화수소를 줄이며, 결과적으로 반응기의 수명까지 연장할 수 있다. According to the present invention, by multiplying chlorine into the upper position of ethylene, the reaction productivity can be increased, the unreacted hydrogen chloride can be reduced, and consequently the lifetime of the reactor can be extended.
도 1은 종래 발명(즉, 비교 예 1)에서 사용된 제조 장치의 개략도이고,
도 2는 본 발명에서 사용된 제조 장치의 개략도이다. 1 is a schematic diagram of a manufacturing apparatus used in the conventional invention (ie, Comparative Example 1),
2 is a schematic diagram of a manufacturing apparatus used in the present invention.
이하, 본 발명의 이해를 돕기 위하여 바람직한 실시 예를 제시하나, 하기 실시 예는 본 발명을 예시하는 것일 뿐 본 발명의 범위가 한정되는 것은 아니다.
Hereinafter, preferred examples are provided to aid the understanding of the present invention, but the following examples are merely to illustrate the present invention, but the scope of the present invention is not limited.
실시 예 1Example 1
도 2에 도시한 반응기 내 순환 용액 내 1,2-디클로로에탄의 순도 85 %에서 에틸렌 (6)과 염소 (7)를 선속도 (velocity) 기준으로 1.2:1의 비율로 투입하고 120 ℃하에 반응을 수행하였다. 순환용매인 1,2-디클로로에탄의 순도는 90 %이며, 순환 용매 내 촉매로서 FeCl3는 농도 500 ppm으로 하여 반응을 수행하였다.
Ethylene (6) and chlorine (7) were introduced at a rate of 1.2: 1 based on the velocity at a rate of 85% of 1,2-dichloroethane in the circulating solution in the reactor shown in FIG. 2 and reacted at 120 ° C. Was performed. The purity of the circulating
이때 염소 (7)의 투입 비율은 하단부, 중간부, 상단부의 3단을 통하여 투입하는 비가 3:1:1이며, 생성된 기체 1,2-디클로로에탄 (EDC)의 선택도 (순도)와 주요 부산물 1,1,2-트리클로로에탄 (TCE) 함량(wt%) 및 미반응된 염소 농도(ppm)를 측정하여 하기 표 1에 정리하였다.
At this time, the ratio of chlorine (7) is 3: 1: 1 in the ratio of the three stages of the lower end, the middle part, and the upper end, and the selectivity (purity) and the majority of the produced
비교 예 1Comparative Example 1
상기 실시 예 1에서 염소를 하단부에만 투입(1:0:0)한 것을 제외하고는 실시 예 1과 동일한 공정을 반복하고 생성된 기체 EDC의 선택도(순도)와 주요 부산물 TCE 함량(wt%) 및 미반응된 염소 농도(ppm)를 하기표 1에 함께 정리하였다.
The same process as in Example 1 was repeated except that chlorine was injected into the lower end of Example 1 (1: 0: 0), and the selectivity (purity) and the main by-product TCE content (wt%) of the generated gas EDC were repeated. And unreacted chlorine concentration (ppm) are summarized together in Table 1 below.
실시예Example 2 2
상기 실시 예 1에서 염소를 하단부:중간부:상단부에서 4:1:0으로 투입한 것을 제외하고는 실시 예 1과 동일한 공정을 반복하고 생성된 기체 EDC의 선택도(순도)와 주요 부산물 TCE 함량(wt%) 및 미반응된 염소 농도(ppm)를 하기 표 1에 함께 정리하였다. The same process as in Example 1 was repeated except that chlorine was added at 4: 1: 0 in the lower part: the middle part: the upper part in Example 1, and the selectivity (purity) and the main by-product TCE content of the generated gas EDC were repeated. (wt%) and unreacted chlorine concentration (ppm) are summarized together in Table 1 below.
(하단부:중간부:상단부)Chlorine input ratio
(Lower part: middle part: upper part)
상기 표에서 보듯이, 본 발명에 따른 반응물 투입 방법을 적용할 경우 생성된 EDC의 순도가 개선되고 부산물은 줄일 수 있을 뿐 아니라 미반응 염화수소 농도도 현저하게 저감되므로 반응기의 수명까지 개선할 수 있다.
As shown in the above table, when the reactant input method according to the present invention is applied, the purity of the generated EDC is improved and the by-products are not only reduced, but the unreacted hydrogen chloride concentration is significantly reduced, thereby improving the lifetime of the reactor.
1… 반응기
2… 기체 EDC
3… 액체 EDC
4… 순환 액체 EDC
5… 루프
6… 에틸렌
7… 염소
8… 스파져One… Reactor
2… Gas EDC
3 ... Liquid EDC
4… Circulating Liquid EDC
5 ... Loop
6 ... Ethylene
7 ... Goat
8… Sparger
Claims (10)
상기 염소의 투입 위치를 조절하는 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
In the method for producing 1,2-dichloroethane by reacting ethylene and chlorine in the presence of a circulating solvent containing 1,2-dichloroethane and a catalyst,
Method for producing 1,2-dichloroethane, characterized in that for adjusting the input position of the chlorine.
상기 염소는 에틸렌보다 상부 위치에서 분리 다단 주입되는 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
The method of claim 1,
The chlorine is a method of producing 1,2-dichloroethane, characterized in that the separation multi-stage injection at a position above ethylene.
상기 분리 다단 주입은 2 내지 3개의 다단 스파져를 사용하여 수행되는 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
The method of claim 2,
The separation multi-stage injection is a method for producing 1,2-dichloroethane, characterized in that it is carried out using two to three multi-stage sparger.
상기 분리 다단 주입은 하단부:중간부:상단부의 다단을 통해 3:1:1의 중량비로 투입되는 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
The method of claim 3, wherein
The separation multi-stage injection is a method of producing 1,2-dichloroethane, characterized in that the input ratio in the weight ratio of 3: 1: 1 through the multi-stage of the lower end: middle part.
상기 분리 다단 주입은 하단부:중간부:상단부의 다단을 통해 4:1:0의 중량비로 투입되는 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
The method of claim 3, wherein
The separation multi-stage injection is a method of producing 1,2-dichloroethane, characterized in that the input ratio of 4: 1: 0 through the multi-stage of the lower end: middle part: upper end.
상기 1,2-디클로로에탄의 순도는 85 내지 99.9 %이고, 에틸렌/염소 비율은 1.0 내지 1.2, 반응 온도는 100 내지 125 ℃인 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
The method of claim 1,
Purity of the 1,2-dichloroethane is 85 to 99.9%, the ethylene / chlorine ratio is 1.0 to 1.2, the reaction temperature is 100 to 125 ℃ method for producing 1,2-dichloroethane.
상기 1,2-디클로로에탄의 순도는 90 내지 99 %이고, 에틸렌/염소 비율은 1.05 내지 1.15, 반응 온도는 110 내지 120 ℃인 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
The method according to claim 6,
Purity of the 1,2-dichloroethane is 90 to 99%, the ethylene / chlorine ratio is 1.05 to 1.15, the reaction temperature is 110 to 120 ℃ manufacturing method of 1,2-dichloroethane.
상기 촉매로는 FeCl3 300 내지 3000 ppm을 사용하는 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
The method of claim 1,
Method for producing 1,2-dichloroethane, characterized in that 300 to 3000 ppm of FeCl 3 as the catalyst.
상기 촉매는 반응기 내부에서 생성되거나 별도로 투입되는 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.
The method of claim 8,
The catalyst is produced in the reactor or a method for producing 1,2-dichloroethane, characterized in that it is added separately.
상기 방법에 따른 부산물로 발생하는 1,1,2-트리클로로에탄의 함량은 1.5 내지 1.8 중량%인 것을 특징으로 하는 1,2-디클로로에탄의 제조방법.The method of claim 1,
Method for producing 1,2-dichloroethane, characterized in that the content of 1,1,2-trichloroethane generated as a by-product according to the method is 1.5 to 1.8% by weight.
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| CN107074693A (en) * | 2014-07-29 | 2017-08-18 | 蒂森克虏伯工业解决方案股份公司 | Method and apparatus for the synthesis of 1,2-dichloroethane |
| US9981890B2 (en) | 2014-07-29 | 2018-05-29 | Thyssenkrupp Industrial Solutions Ag | Method and a device for synthesizing 1.2-dichloroethane |
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