WO2012091397A2 - 고순도 2-에틸헥실-아크릴레이트 생산을 위한 분리벽형 증류탑 및 이를 이용한 제조방법 - Google Patents
고순도 2-에틸헥실-아크릴레이트 생산을 위한 분리벽형 증류탑 및 이를 이용한 제조방법 Download PDFInfo
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- WO2012091397A2 WO2012091397A2 PCT/KR2011/010132 KR2011010132W WO2012091397A2 WO 2012091397 A2 WO2012091397 A2 WO 2012091397A2 KR 2011010132 W KR2011010132 W KR 2011010132W WO 2012091397 A2 WO2012091397 A2 WO 2012091397A2
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- dividing wall
- distillation column
- ethylhexyl
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C67/54—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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- 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
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
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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
- Y02P20/10—Process efficiency
Definitions
- the present invention relates to a dividing wall distillation column for producing high-purity 2-ethylhexyl-acrylate and a manufacturing method using the same.
- Various raw materials such as crude oil are usually a mixture of many compounds, so they are rarely used in industry by itself, and are usually used after being separated into each compound.
- a typical chemical process for separating a mixture is distillation.
- the distillation process divides the high boiling point component and the low boiling point component, one distillation column (n-1) is used which is one less than the number n of components of the mixture to be separated. That is, in the conventional distillation industry, the process for separating high-purity products from crude raw materials uses two continuous distillation column structures.
- the conventional distillation process is as shown in FIG.
- the conventional process is a two tower method in which the lowest boiling point component (D) is separated from the first tower 11 and the middle boiling point component (S) and the high boiling point component (B) are separated from the second tower 21.
- the composition profile in the first column in the conventional two-column distillation method which is a conventional alcohol distillation process, is shown in FIG. 2.
- remixing of the middle boiling point (B) material generally occurs in the first column lower region.
- the composition profile in the first column is shown in FIG. 3.
- FIG. 3 it can be seen that re-mixing occurs in the first column lower region even in the case of 2-ethylhexyl-acrylate.
- the Petlyuk distillation column arranges the pre-separator 12 and the main separator 22 in a thermally integrated structure to separate low-boiling material and high-boiling material from the pre-separator first, and then to the top part of the pre-separator.
- the bottom part is respectively introduced into the feed stage of the main separator to separate the low boiling point (D), the middle boiling point (S), the high boiling point (B) material in the main separator.
- This structure makes the distillation curve in the Petlyuk distillation column similar to the equilibrium distillation curve, making the energy efficiency higher.
- the design and operation of the process is not easy and in particular, it is difficult to balance the pressure in the tower.
- the present invention provides a dividing wall distillation column for producing high-purity 2-ethylhexyl-acrylate and a manufacturing method using the same.
- the present invention a condenser; Reboiling; And a main tower including a partition wall, wherein the main tower is divided into a tower top zone, an upper feed zone, an upper outlet zone, a lower feed zone, a lower outlet zone, and a tower bottom zone, and includes one or more inflow streams and three or more outflow streams.
- the inlet stream is the feed containing crude 2-ethylhexyl-acrylate into the feed intermediate stage where the upper feed zone and the lower feed zone of the main column meet, and at least one of the outlet streams is 2-ethylhexyl-acrylic
- the present invention provides a distillation column type distillation column, which is a rate flow, and a method for producing high purity 2-ethylhexyl-acrylate using the same.
- the dividing wall distillation column according to the present invention can exert the effect of two distillation columns with one distillation column, and can save energy compared to the conventional process equipment for producing high-purity 2-ethylhexyl-acrylate, and the equipment cost of the equipment Can be reduced.
- 1 is a schematic representation of a conventional distillation process for producing high purity 2-ethylhexyl-acrylate
- Figure 2 shows the composition profile in the first column in the distillation process of a two-column column
- Figure 3 shows the composition profile of 2-ethylhexyl-acrylate in the first column in the distillation process of a two-column column
- FIG. 5 is a schematic diagram showing the structure of a dividing wall distillation column according to an embodiment of the present invention.
- FIG. 6 shows a composition profile in a column of a dividing wall distillation column according to an embodiment of the present invention
- FIG. 7 is a schematic diagram showing a process of distilling 2-ethylhexyl-acrylate using a dividing wall distillation column according to an embodiment of the present invention
- FIG. 8 is a schematic diagram showing a process of distilling 2-ethylhexyl-acrylate using a two column column distillation column.
- a dividing wall type distillation column comprising a main column including a condenser, a reboiler and a dividing wall,
- the main tower is divided into a tower top zone, an upper feed zone, an upper outlet zone, a lower supply zone, a lower outlet zone and a tower bottom zone, and has one or more inflow streams and three or more outflow streams.
- the inflow stream is where the raw material (F) containing crude 2-ethylhexyl-acrylate enters the feed intermediate stage (NR1), which is in contact with the upper feed zone and the lower feed zone of the main column,
- At least one of the effluent streams is characterized as a 2-ethylhexyl-acrylate stream.
- the dividing wall column is similar to the PETLYUK distillation column in terms of thermodynamics, but the dividing wall column is formed by integrating a preliminary separator into the main separator by installing a dividing wall in the column from a structural point of view.
- the distillation column of this structure is easy to operate by naturally relieving the pressure balance between the preliminary separator and the main separator and the operational difficulties caused by the distillation column. You have an advantage.
- the present invention is a dividing wall distillation column comprising a main column including a condenser, a reboiler, and a dividing wall,
- the main tower is divided into a tower top zone, an upper supply zone, an upper outlet zone, a lower supply zone, a lower outlet zone and a tower bottom zone,
- the raw material (F) containing crude 2-ethylhexyl-acrylate flows into the feed intermediate stage (NR1), which is in contact with the upper feed zone and the lower feed zone of the main column, and the low boiling point component (D) flows out of the tower top zone,
- the high boiling point component (B) flows out of the top bottom zone, and the middle boiling point component (S) flows out of the outflow intermediate stage (NR2) in contact with the upper outflow zone and the lower outflow zone,
- the middle boiling point component provides a dividing wall distillation column, characterized in that substantially 2-ethylhexyl-acrylate.
- the raw material (F) may be 80% by weight or more of 2-ethylhexyl-acrylate 2-ethylhexyl-acrylate.
- the dividing wall distillation column includes a main tower 1 and a condenser 31 and a reboiler 41 connected to the top and bottom of the main tower 1, respectively.
- the condenser 31 is a device that takes away the heat of vaporization of the gaseous mixture to condense, it can be used without limitation the condenser used in the conventional chemical engineering device.
- the reboiler 41 is a device for providing a vaporization heat to the mixture in the liquid state to vaporize, it can be used without limitation the reboiler used in the conventional chemical engineering device.
- the main tower 1 can be largely divided into six sections.
- Pagoda section 100 refers to the area of the top of the main tower without a partition wall.
- the upper feed zone 200 is a region in which one side is partitioned by the dividing wall, and is a subregion located above the inflow (raw material) flow.
- the upper outlet area 300 is an area in which one surface is partitioned by the dividing wall, and is a sub area located above the effluent stream.
- the lower feed zone 400 is an area where one surface is partitioned by the dividing wall, and is a sub area located below the inflow stream.
- the lower outlet area 500 is an area where one surface is partitioned by the dividing wall, and is a sub area located below the effluent flow.
- the tower bottom region 600 means the lower region of the main column without a partition wall.
- the main column 1 also has at least one inflow stream and at least three outflow streams.
- the inlet flow is the feed intermediate (NR1) where the raw material (F), which is crude 2-ethylhexyl-acrylate (crude 2-EHA), is in contact with the upper feed zone (200) and the lower feed zone (400) of the main column (1). It includes the flow into.
- the outflow flow the low boiling point component (D) flowing out from the tower top section 100, the high boiling point component (B) flowing out from the top bottom zone 600, the outflow contact with the upper outlet 300 and lower outlet 500 It may include a middle boiling point component (S) flowing out to the intermediate stage (NR2).
- the middle boiling point component (S) which flows out to the middle stage of the outflow (NR2) may be substantially 2-ethylhexyl-acrylate.
- 'crude 2-ethylhexyl-acrylate raw material' refers to a mixture whose main component is 2-ethylhexyl-acrylate, and refers to a target (distillation target) of the distillation process, wherein the 'main component' is It refers to the one component which contains the most among the individual components of each mixture.
- the higher the 2-ethylhexyl-acrylate content of the crude 2-ethylhexyl-acrylate raw material is preferable, and the higher purity 2-ethylhexyl-acrylate is 99% by weight or more. It is preferable that it is 80 weight% or more in order to obtain.
- substantially 2-ethylhexyl-acrylate means that the mixture itself can be regarded as substantially 2-ethylhexyl-acrylate, specifically, 2-ethylhexyl It refers to an acrylate-based component, having a higher 2-ethylhexyl-acrylate content relative to the feedstock and a 2-ethylhexyl-acrylate component in excess of at least 90% by weight in the total mixture.
- the reason why the dividing wall distillation process requires less energy than the conventional continuous two-stage distillation process can be interpreted as a structural difference.
- the space divided by the dividing wall acts as a preliminary separator, so that the liquid composition is almost in line with the equilibrium distillation curve due to the separation of the high boiling point material and the low boiling point material, and the remixing effect is suppressed. Thermodynamic efficiency is improved.
- the upper feed zone and the lower feed zone play a similar role to the preliminary separator of the conventional process. That is, the upper supply zone and the lower supply zone may be collectively referred to as a preliminary separation zone.
- Raw material flowing into the preliminary separation zone is separated into low boiling point material and high boiling point material.
- Some of the low boiling point components and the high boiling point components separated from the preliminary separation zone flow into the top top zone, and some of the low boiling point components and the high boiling point components flow into the upper outlet zone and the lower outlet zone.
- the upper and lower outlet zones serve as the main separator of the conventional process. That is, the upper outlet area and the lower outlet area may be collectively referred to as the main separation area.
- the main separation area In the upper portion of the separation wall of the main separation region, mainly the low boiling point material and the middle boiling point material are separated, and in the lower part, the middle boiling point material and the high boiling point material are mainly separated.
- composition profile in the dividing wall distillation column according to an embodiment of the present invention is shown in FIG. 6.
- the low boiling point component passes through the tower top section and the condenser, and part of it is produced as a low boiling point product (D), and the rest is returned to the tower top section at the liquid flow rate (LD).
- LD liquid flow rate
- B high boiling point product
- B the high boiling point product
- VB gas phase flow rate
- the design of the combined column distillation column system with the dividing wall is based on the design of the existing combined column distillation column and the minimum tower design.
- the efficiency of the distillation column is maximum when the liquid composition distribution of the column distillation stage is similar to the equilibrium distillation curve, so the first stage distillation system is designed assuming that the distillation column is operated by conversion flow operation.
- the upper supply zone and the lower supply zone are designed, and the upper outlet zone and the lower outlet zone are designed by the stepwise equilibrium design method starting from the concentration of the middle boiling point product.
- the liquid composition in the tower was calculated from the middle of the tower to the top, and the liquid phase inside the tower was sequentially calculated by the method of equilibrium composition from the middle of the tower to the bottom of the lower outlet area serving as the main separator. .
- the number of stages having the composition of the raw material supply stage and the product is counted as the upper feed zone and the lower feed zone serving as the preliminary separator, and the upper outlet zone and the lower outlet zone serving as the main separator, respectively. I can figure it out.
- the number of stages of the tower obtained here is the theoretical number of stages, and since the number of stages in the actual tower may vary according to conventional design criteria.
- the number of stages respectively provided in the tower top zone, the upper feed zone, the upper outflow zone, the lower feed zone, the lower outflow zone and the bottom bottom zone is 90 to 140% of the theoretical stage calculated by the distillation curve. It can be within. If it is less than 90% of the calculated theoretical number, the low boiling point and high boiling point material may not be separated in the preliminary separation zone. If it exceeds 140%, the energy saving effect does not increase any more because it is the minimum reflux ratio area. It is not desirable because it is increased.
- the length of the dividing wall installed inside the main column is the upper supply section and the lower supply section; Alternatively, the length is determined by the number of stages calculated according to the distillation curves of the upper and lower outlet zones.
- the optimal partition wall section in a distillation column type distillation column there are a variety of methods for determining theoretical section and reflux amount by determining the partition wall section by the equilibrium distillation curve method for the liquid composition between the preliminary section and the main section.
- the theoretical singular was obtained by using the Fenske-Underwood equation.
- the Penske-Underwood equation is known to one of ordinary skill in the art.
- the length of the dividing wall may be in the range of 40 to 85% of the total theoretical stage of the top section, the upper feed section, the bottom outlet section and the bottom section calculated by the distillation curve. If it is less than 40%, some of the low boiling point material may fall down into the main separator product in the preliminary separation zone, and if it is more than 85%, the liquid / gas and medium / high boiling point of the low boiling point / medium point material inside the column. Difficulties in maintaining a good equilibrium flow of the liquid / phase of the material can lead to problems in column fabrication.
- the operating conditions of the dividing wall distillation column to prepare high-purity 2-ethylhexyl-acrylate are as follows.
- the temperature of the overhead zone is preferably in the range of 88-98 ° C. at a pressure of 15-25 torr of overhead tower. If it is below 88 °C, low boiling point material may sag below the preliminary separation zone, affecting product purity. If it exceeds 98 °C, high boiling point material (HEAVIES) rises above the preliminary separation zone and affect product purity. There is concern.
- HEAVIES high boiling point material
- the temperature of the column bottom zone is preferably in the range of 138 to 148 ° C at a pressure in the column top section of 15 to 25 torr. If it is below 138 ° C, the product's middle boiling point material falls to the bottom and the product yield decreases. If it exceeds 148 ° C, HEVIES may flow sideways with the product's middle boiling point material.
- the temperature of the outflow intermediate stage (NR2) at which the upper outlet region and the lower outlet region are in contact with each other and the middle boiling point S component flows out is in the range of 124 to 134 ° C. at the pressure of the top region of 15 to 25 torr. desirable. If it is less than 124 °C low boiling point material is not easy to remove, if it exceeds 134 °C it is not easy to remove the high boiling point material can have a big impact on product purity.
- the temperature range may be changed.
- the upper limit temperature and the lower limit temperature tend to increase.
- the pressure in the top zone is about 15 torr, about 83 to about 93 ° C in the top zone, about 135 to about 145 ° C in the top bottom zone, and about 120 to about 130 ° C in the middle effluent stream (NR2).
- NR2 middle effluent stream
- the temperature of the top zone may range from a lower limit temperature (T 1a ) to an upper limit temperature (T 2a ) according to Equation 1 below.
- T 1a -0.02P 2 + 1.7P + 62
- T 1a And T 2a Is the temperature, the unit is °C; P is the pressure in the tower top section, unit is torr ; 1 ⁇ P ⁇ 70)
- the temperature of the column bottom zone may be in the range of the lower limit temperature T 1b to the upper limit temperature T 2b according to Equation 2 below.
- T 1b -0.0267P 2 + 1.5333P + 118
- T 1b And T 2b Is the temperature, the unit is °C; P is the pressure in the tower top section, unit is torr ; 1 ⁇ P ⁇ 70)
- the temperature of the upper outflow zone and the lower outflow zone is provided in the contact position intermediate boiling point (S) simple (NR2) of the outlet which component outlet is to the lower limit temperature according to the equation 3 (T 1c) to the upper limit temperature (T 2c ) range.
- T 1c -0.0267P 2 + 1.7333P + 100
- T 1c And T 2c Is the temperature, the unit is °C; P is the pressure in the tower top section, unit is torr ; 0.1 ⁇ P ⁇ 70)
- Dividing wall thermocomposition distillation column system aims to improve the tower efficiency of the distillation system for the three-component mixture, this system is similar to the distillation system of equilibrium distillation system of high efficiency equilibrium distillation It has the same effect as that composed of two distillation towers to form a space which functions as a pre separator and a main separator having a composition distribution.
- the present invention provides a method for producing 2-ethylhexyl-acrylate using the dividing wall distillation column.
- High-purity 2-ethylhexyl-acrylate can be produced by providing crude 2-ethylhexyl-acrylate raw material in a dividing wall distillation column and fractionally distilling 2-ethylhexyl-acrylate.
- the dividing wall distillation column includes a main column including a condenser, a reboiler and a dividing wall,
- the main tower is divided into a tower top zone, an upper feed zone, an upper outlet zone, a lower supply zone, a lower outlet zone and a tower bottom zone, and has one or more inflow streams and three or more outflow streams.
- the inflow stream is where the raw material (F) containing crude 2-ethylhexyl-acrylate enters the feed intermediate stage (NR1), which is in contact with the upper feed zone and the lower feed zone of the main column,
- the outflow flow includes the low boiling point component (D) flowing out from the top top zone, the high boiling point component (B) flowing out from the top bottom zone, and the middle boiling point component flowing out to the outflow intermediate end (NR2) in contact with the upper outlet zone and the lower outlet zone ( S), and the stream exiting effluent intermediate (NR2) may be substantially 2-ethylhexyl-acrylate.
- a dividing wall distillation column (DWC) was designed and manufactured and operated. It was confirmed that the composition of the required product was obtained through actual operation.
- the comparative example uses two distillation columns without a conventional dividing wall, and the example uses one distillation column with a dividing wall.
- FIGS. 7 and 8 illustrate examples and comparative examples of the present invention, respectively.
- 7 illustrates a case of using a dividing wall distillation column according to an embodiment of the present invention
- FIG. 8 illustrates a case of using a distillation column including two conventional columns.
- Numbers 1 to 8 in FIGS. 7 and 8 are identification numbers representing individual streams shown in the drawings of the examples and the comparative examples, respectively.
- Table 3 shows the flow conditions and composition according to the embodiment
- Table 4 shows the flow conditions and composition according to the comparative example.
- the separation wall type steam tower according to the embodiment was able to more efficiently obtain high purity 2-ethylhexyl-acrylate of 99.9 wt% due to the removal of remixing and the increase in separation efficiency. Additional rectification recycle steps of 2-ethylhexyl-acrylate due to increased product purity can be reduced and productivity can be improved.
- Table 5 is the result of measuring the energy consumption according to the Example (DWC) and Comparative Example (existing), and calculated the reduction rate.
- Comparative example using an existing distillation column requires two columns and four heat exchangers, but the dividing wall distillation column according to the present invention may be composed of one column and two heat exchangers. Therefore, the dividing wall distillation column according to an embodiment of the present invention can reduce about 30% of the existing investment in terms of investment cost. In particular, the energy saving rate was significantly reduced to 25.9%.
- main tower 11 first tower
- tower top zone 200 upper feed zone
- the dividing wall distillation column according to the present invention can be variously used in the field using 2-ethylhexyl-acrylate.
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Abstract
Description
P ≒ 20 torr | ||
하한 온도(℃) | 상한 온도(℃) | |
탑정구역 | 88 | 98 |
탑저구역 | 138 | 148 |
유출중간단(NR2) | 124 | 134 |
P ≒ 15 torr | ||
하한 온도(℃) | 상한 온도(℃) | |
탑정구역 | 83 | 93 |
탑저구역 | 135 | 145 |
유출중간단(NR2) | 120 | 130 |
P ≒ 30 torr | ||
하한 온도(℃) | 상한 온도(℃) | |
탑정구역 | 95 | 105 |
탑저구역 | 140 | 150 |
유출중간단(NR2) | 128 | 138 |
항목 | 이론단수 | |
실시예 | 탑정 구역(100) | 8 |
상부 공급구역(200) | 9 | |
상부 유출구역(300) | 10 | |
하부 공급구역(400) | 18 | |
하부 유출구역(500) | 5 | |
탑저 구역(600) | 15 | |
비교예 | 첫번째 컬럼 | 18 |
두번째 컬럼 | 20 |
실시예 | 흐름 번호 | 1 | 2 | 3 | 4 | 5 |
조건 | 온도(℃) | 50.0 | 55.2 | 55.2 | 77.2 | 93.9 |
압력(torr) | 1471.1 | 35.0 | 35.0 | 69.8 | 90.0 | |
유량(kg/hr) | 5129.6 | 8063.5 | 610.0 | 3920.0 | 599.6 | |
조성 | 저비점(중량%) | 15.00 | 75.00 | 75.00 | 0.00 | 0.00 |
중비점(중량%) | 81.10 | 25.00 | 25.00 | 100.00 | 76.90 | |
고비점(중량%) | 3.90 | 0.00 | 0.00 | 0.00 | 23.10 | |
합계(중량%) | 100 | 100 | 100 | 100 | 100 |
비교예 | 흐름 번호 | 1 | 2 | 3 | 4 | 5 | 6 | 7 |
조건 | 온도(℃) | 60.0 | 55.2 | 55.2 | 84.7 | 62.5 | 62.6 | 96.5 |
압력(torr) | 1471.1 | 35.0 | 35.0 | 2966.7 | 35.0 | 35.0 | 100.0 | |
유량(kg/hr) | 6129.6 | 6464.9 | 610.0 | 4519.6 | 3959.2 | 3920.0 | 699.6 | |
조성 | 저비점(중량%) | 15.00 | 75.00 | 75.00 | 0.00 | 0.00 | 0.00 | 0.00 |
중비점(중량%) | 81.10 | 25.00 | 25.00 | 95.10 | 100.00 | 100.00 | 77.00 | |
고비점(중량%) | 3.90 | 0.00 | 0.00 | 4.90 | 0.00 | 0.00 | 23.00 | |
합계(중량%) | 100 | 100 | 100 | 100 | 100 | 100 | 100 |
비교예 | 실시예 | 절감량(MMKcal/hr) | 절감율(%) | |||
에너지 소비량(MMKcal/hr) | 첫번째 컬럼 | 두번째 컬럼 | 합계 | 0.43 | 0.15 | 25.9 |
0.39 | 0.19 | 0.58 |
Claims (10)
- 응축기; 재비기; 및 분리벽을 포함하는 주탑을 포함하며,주탑은 탑정구역, 상부 공급구역, 상부 유출구역, 하부 공급구역, 하부 유출구역 및 탑저구역으로 구분되고,1 개 이상의 유입 흐름과 3 개 이상의 유출 흐름을 가지고,유입 흐름은 크루드 2-에틸헥실-아크릴레이트가 함유된 원료가 주탑의 상부 공급구역 및 하부 공급구역이 접하는 공급 중간단으로 유입되는 것이고,유출 흐름 중 하나 이상은 2-에틸헥실-아크릴레이트 흐름인 분리벽형 증류탑.
- 제 1 항에 있어서,저비점 성분은 탑정구역에서 유출되고, 고비점 성분(B)은 탑저구역에서 유출되고, 중비점 성분은 상부 유출구역 및 하부 유출구역이 접하는 유출중간단으로 유출되고,유출중간단으로 유출되는 흐름은 2-에틸헥실-아크릴레이트인 분리벽형 증류탑.
- 제 1 항에 있어서,상기 원료는 2-에틸헥실-아크릴레이트의 함량이 80 중량% 이상인 분리벽형 증류탑.
- 제 1 항에 있어서,주탑의 탑정구역, 상부 유출구역, 하부 공급구역, 하부 유출구역 및 탑저구역에 구비되는 각각의 단수는 증류곡선에 의해 산출되는 이론단수의 90 내지 140% 범위인 분리벽형 증류탑.
- 제 1 항에 있어서,분리벽의 길이는 상부 공급구역 및 하부 공급구역, 또는 상부 유출구역과 하부 유출구역이 포함하는 단수에 따라 그 길이가 결정되는 분리벽형 증류탑.
- 제 1 항에 있어서,분리벽의 길이는 증류곡선에 의해 산출되는 탑정구역, 상부 공급구역, 하부 유출구역 및 탑저구역 전체 이론단수의 40 내지 85% 범위인 분리벽형 증류탑.
- 제 1 항에 있어서,탑정구역의 온도는 하기 수학식 1을 따르는 하한온도(T1a) 내지 상한온도(T2a) 범위 이내인 분리벽형 증류탑:[수학식 1]T1a= -0.02P2 + 1.7P + 62T2a= -0.02P2 + 1.7P + 72(상기 식에서, T1a 및 T2a는 온도로서, 단위는 ℃; P는 탑정구역의 압력으로 단위는 torr; 1≤P≤70).
- 제 1 항에 있어서,탑저구역의 온도는 하기 수학식 2를 따르는 하한온도(T1b) 내지 상한온도(T2b) 범위 이내인 분리벽형 증류탑:[수학식 2]T1b= -0.0267P2 + 1.5333P + 118T2b= -0.0267P2 + 1.5333P + 128(상기 식에서, T1b 및 T2b는 온도로서, 단위는 ℃; P는 탑정구역의 압력으로 단위는 torr; 1≤P≤70).
- 제 1 항에 있어서,상부 유출구역 및 하부 유출구역이 접하는 위치에 구비되고 중비점 성분이 유출되는 중간단의 온도는 하기 수학식 3을 따르는 하한온도(T1c) 내지 상한온도(T2c) 범위 이내인 분리벽형 증류탑:[수학식 3]T1c= -0.0267P2 + 1.7333P + 100T2c= -0.0267P2 + 1.7333P + 110(상기 식에서, T1c 및 T2c는 온도로서, 단위는 ℃; P는 탑정구역의 압력으로 단위는 torr; 1≤P≤70).
- 제 1 항 내지 제 9 항 중 어느 한 항에 따른 분리벽형 증류탑을 이용하여 2-에틸헥실-아크릴레이트를 제조하는 방법.
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WO2012091397A3 (ko) | 2012-11-08 |
JP5696954B2 (ja) | 2015-04-08 |
EP2659943B1 (en) | 2017-09-06 |
US8894821B2 (en) | 2014-11-25 |
US20130284586A1 (en) | 2013-10-31 |
KR101496488B1 (ko) | 2015-02-26 |
CN103298531A (zh) | 2013-09-11 |
KR20120076193A (ko) | 2012-07-09 |
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