WO2010107283A2 - 고순도 2-에틸헥산올 생산을 위한 분리벽형 증류탑 및 이를 이용한 분별증류방법 - Google Patents
고순도 2-에틸헥산올 생산을 위한 분리벽형 증류탑 및 이를 이용한 분별증류방법 Download PDFInfo
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- WO2010107283A2 WO2010107283A2 PCT/KR2010/001725 KR2010001725W WO2010107283A2 WO 2010107283 A2 WO2010107283 A2 WO 2010107283A2 KR 2010001725 W KR2010001725 W KR 2010001725W WO 2010107283 A2 WO2010107283 A2 WO 2010107283A2
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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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- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
- C07C31/125—Monohydroxylic acyclic alcohols containing five to twenty-two carbon atoms
Definitions
- the present invention relates to a dividing wall distillation column for producing high-purity 2-ethylhexanol and a fractional distillation method using the same.
- distillation column n-1
- n-1 one distillation column 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 the three-component mixture uses a continuous two distillation column structure.
- 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 is shown in FIG. 2.
- remixing of the middle boiling point component S generally occurs in the first column lower region.
- the composition profile in the first column is shown in FIG. 3.
- octanol also causes remixing of octanol in the lower region of the first column.
- a representative example of improving the separation efficiency by the heat integration structure is a Petlyuk distillation column structure as shown in FIG.
- the pre-separator 12 and the main separator 22 are arranged in a thermally integrated structure to separate low-boiling components and high-boiling components from the pre-separator first, and then the top and bottom portions of the pre-separator are mainly separated. It is introduced into the feed stage of the separator to separate the low boiling point, middle boiling point, and high boiling point components in the main separator, respectively.
- This structure makes the energy distillation curve in the Petlyuk distillation column similar to the equilibrium distillation curve.
- the design and operation of the process is not easy and in particular, it is difficult to balance the pressure in the tower.
- a dividing wall column (DWC) has been proposed.
- the dividing wall distillation column is similar to the Petlyuk distillation column in terms of thermodynamics, but from the structural point of view, the dividing wall is installed in the tower to integrate the preliminary separator of the Petlyuk distillation column into the main separator.
- This structure facilitates operation by relieving the pressure balance between the preliminary and main separators of the Petlyuk distillation column and the operational difficulties, and also reduces the investment cost by integrating the two distillation columns into one. It has a big advantage.
- the above-described technique is carried out by passing a by-product of a plant producing 2-ethylhexanol from butyl aldehyde by aldol condensation reaction and hydrogenation reaction through two multistage distillation columns, 2-ethylhexanol and 2-ethylhexyl-2-ethylhexa.
- the by-product is 100 parts by weight of 2-ethylhexanol, 2 to 6 parts by weight of butyl aldehyde trimer (TRIMER), 7 to 12 parts by weight of 2-ethylhexyl-2-ethylhexanoate Part by weight and the high boiling point component of 0.01 to 0.3 parts by weight, recovering 2-ethylhexanol by passing the by-product through the first multi-stage distillation column and the residue in the second multi-stage distillation column operating pressure is 980.665 to 9806.650 kPa
- the operating temperature relates to a method comprising the step of recovering 2-ethylhexyl-2-ethylhexanoate by distillation under operating conditions of 150 to 200 °C.
- This technique uses two columns similarly to the conventional process, and differs greatly from the present invention in that it does not relate to a distillation column including a dividing wall.
- the dividing wall type column has a lack of flexibility in operating conditions due to its structural characteristics that cannot control the internal circulation flow rate. That is, there is a problem that accurate simulation and structure determination are necessary in the initial design stage of the distillation column.
- the present invention is to solve the above problems, to provide a dividing wall distillation column and a method of operation thereof designed for 2-ethylhexanol purification to reduce the energy used as well as to reduce the equipment cost.
- the present invention has been made to solve the above problems of the prior art,
- a dividing wall distillation column comprising a main column having 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,
- Crude 2-ethylhexanol raw material (F) flows into the feed intermediate stage (NR1) in contact with the upper feed zone and the lower feed zone, the low boiling point component (D) flows out of the tower top zone, and the high boiling point component ( B) flows out from the bottom zone, the middle boiling point component (S) flows out to the outflow intermediate stage (NR2) in contact with the upper outflow zone and the bottom outflow zone,
- the middle boiling point component is a dividing wall distillation column, characterized in that 2-ethylhexanol.
- the raw material (F) provides a dividing wall distillation column, characterized in that the 2-ethylhexanol content is 90% by weight or more.
- the number of stages provided in the tower zone, the upper feed zone, the upper outlet zone, the lower feed zone, the lower outlet zone, and the tower bottom zone is 80 to 145% of the theoretical stage calculated by the distillation curve. It provides a dividing wall distillation column, characterized in that within the range.
- the length of the dividing wall provides a dividing wall distillation column, characterized in that the length is determined according to the overall theoretical number of the upper feed zone and the lower feed zone.
- the length of the dividing wall is a dividing wall distillation column, characterized in that within the range of 30 to 85% of the total theoretical number of the top section, the upper feed section, the bottom outlet section and the bottom bottom section calculated by the distillation curve.
- the temperature of the top zone is within the range of 75 to 85 °C under 16.671 kPa pressure.
- the column bottom temperature provides a dividing wall distillation column, characterized in that within the range of 145 to 160 °C under a pressure of 16.671 kPa.
- the temperature of the outlet middle end (NR2) is provided at a position where the upper outlet area and the lower outlet area is in contact and the middle boiling point (S) component is outflow is within the range of 130 to 140 °C under 16.671kPa pressure It provides a dividing wall distillation column.
- the temperature of the top column provides a dividing wall distillation column, characterized in that within the range of the lower limit temperature (T1a) to the upper limit temperature (T2a) according to the following equation when the pressure is not 16.671kPa.
- T1a and T2a are temperatures, units are ° C., P is pressure, units are kPa; 0.981 ⁇ P ⁇ 980.665, P ⁇ 16.671)
- the temperature of the column bottom zone provides a dividing wall distillation column, characterized in that within the range of the lower limit temperature (T1b) to the upper limit temperature (T2b) according to the following equation 2 when the pressure is not 16.671kPa.
- T1b and T2b are temperatures, units are ° C; P is pressure, and kPa is 0.981 ⁇ P ⁇ 980.665, P ⁇ 16.671)
- the temperature of the outflow intermediate stage NR2 provided at a position where 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 according to Equation 3 below when the pressure is not 16.671 kPa. It provides a dividing wall distillation column, characterized in that within the lower limit temperature (T1c) to the upper limit temperature (T2c) range.
- T1c and T2c are temperatures, units are ° C; P is pressure, units are kPa; 0.981 ⁇ P ⁇ 980.665, P ⁇ 16.671)
- the dividing wall type distillation column of the present invention has the effect of two distillation columns in one distillation column, it is possible to reduce the equipment cost of the equipment as well as the energy saving effect in the production of high-purity 2-ethylhexanol. It works.
- 1 is a schematic representation of a conventional distillation process for the separation of a three component mixture.
- 3 is a composition profile in the first column when octanol (2-ethylhexanol) is separated into a middle boiling point component.
- FIG. 4 is a schematic view showing a Petlyuk distillation column structure.
- Figure 5 is a schematic diagram showing the structure of a dividing wall distillation column of the present invention.
- FIG. 6 is a schematic view showing a comparative example.
- FIG. 7 is a schematic diagram showing an embodiment of the present invention.
- a dividing wall distillation column comprising a main column having 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,
- Crude 2-ethylhexanol raw material (F) flows into the feed intermediate stage (NR1) in contact with the upper feed zone and the lower feed zone, the low boiling point component (D) flows out of the tower top zone, and the high boiling point component ( B) flows out from the bottom zone, the middle boiling point component (S) flows out to the outflow intermediate stage (NR2) in contact with the upper outflow zone and the bottom outflow zone,
- the middle boiling point component is characterized in that 2-ethylhexanol.
- FIG. 1 The structure of the dividing wall distillation column of the present invention is shown in FIG.
- the distillation column of the present invention includes a condenser 31 and a reboiler 41.
- the condenser is a device that takes away the heat of vaporization of the gaseous mixture to condense, and can be used without limitation the condenser used in the conventional chemical engineering device.
- the reboiler is a device for providing 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.
- the top section 100 refers to the upper region of the main tower without a partition wall.
- the upper feed zone 200 is an area in which one surface is partitioned by the dividing wall, and is a sub area located above the inflow (raw material) flow.
- the upper outlet area 300 is an area where 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 influent flow.
- 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 zone 600 refers to the lower region of the main tower without a partition wall.
- the pylon has at least one inlet point and at least three outlet points.
- Crude 2-ethylhexanol feed (F) flows into the feed intermediate stage (NR1) where the upper feed zone and the lower feed zone come into contact, and the low boiling point component (D) flows out of the top zone.
- the high boiling point component (B) flows out of the 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 (S) is 2-ethylhexanol.
- crude 2-ethylhexanol raw material refers to a mixture in which the main component is 2-ethylhexanol, which is a target (distillation target) of the distillation process, and the “main component” is the most of the individual components of each mixture.
- the main component is the most of the individual components of each mixture.
- the "middle boiling point component (S) is 2-ethylhexanol” does not mean 100% 2-ethylhexanol, but is substantially 2-ethylhexanol.
- “Substantially 2-ethylhexanol” means that the mixture itself can be regarded as substantially 2-ethylhexanol, specifically, 2-ethylhexanol as a main component, Compared to the higher 2-ethylhexanol content.
- the upper feed zone and the lower feed zone play a similar role to the preliminary separator of the conventional process (ie, the upper feed zone and the lower feed zone may be collectively referred to as the pre-separation zone).
- the three components introduced into the preliminary separation zone are separated into low boiling point components and high boiling point components. A part of the low boiling point component and the high boiling point component separated in the preliminary separation zone flows into the top and bottom zones, and part of the low boiling point component and the high boiling point component flows back into the upper outlet zone and the lower outlet zone and is redistilled.
- the upper outlet zone and the lower outlet zone serve as the main separator of the conventional process (ie, the upper outlet zone and the lower outlet zone collectively may be referred to as the main separator zone).
- the main separator zone In the upper portion of the separation wall of the main separation region, the low boiling point component and the middle boiling point component are mainly separated, and in the lower part, the middle boiling point component and the high boiling point component are mainly separated.
- 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).
- the high boiling point component is passed through the bottom column of the main column and reboiled, and a part of it is produced as a high boiling point product (B), and the rest is returned to the bottom column of the main column at the gas phase flow rate (VB).
- the design of the thermal combined column system with the dividing wall is based on the design of the existing thermal combined column and based on the smallest 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 feed zone and the lower feed 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 mid boiling point product.
- the liquid composition in the tower was calculated from the middle of the tower to the top, and the lower outflow zone, which acts as the main separator, was sequentially calculated by calculating the equilibrium composition method from the middle of the tower to the bottom of the tower starting from the concentration of the middle boiling point product. .
- the upper feed zone and the lower feed zone serving as preliminary separators
- the upper outlet zone and lower outlet zone serving as the main separator, respectively. Since the number of stages of the tower obtained here is the ideal number of stages, the ideal number of stages in the actual tower is preferably 80 to 145% of the number of theoretical stages according to conventional design criteria. If less than 80% of the calculated theoretical number of low boiling point and high boiling point components in the preliminary separation zone may not be well separated, if more than 145% of the minimum reflux ratio region, the energy saving effect does not increase any more, investment costs increase only This is undesirable.
- the length of the dividing wall installed inside the main column is not a fixed value, but varies fluidly according to the type and composition of the raw material to be treated.
- the length is determined according to the overall theoretical number calculated according to the distillation curves of the upper feed zone and the lower feed zone.
- the length of the dividing wall is preferably within the range of 30 to 85% of the total theoretical number of stages of the top zone, the upper feed zone, the bottom outlet zone and the bottom bottom zone calculated by the distillation curve. If it is less than 30%, some of the low boiling point components may fall down in the preliminary separation zone and be included as a product of the main separator, and if it is more than 85%, the liquid / gas and medium / high boiling point components Difficult to maintain a good equilibrium flow of liquid / gas phase may have a problem in column manufacturing.
- the temperature of the column top section of the main column is preferably within the range of 75 to 85 °C under 16.671 kPa pressure. If it is less than 75 °C, low boiling point component (Light) can be drooped under the preliminary separation zone, affecting the purity of the product. If it exceeds 85 °C, high boiling point component (Heavies) will rise to the top of the preliminary separation zone. There is concern.
- the temperature of the column bottom zone of the pylon is preferably within the range of 145 to 160 ° C under 16.671 kPa pressure. If the temperature is less than 145 ° C, the product has a lower boiling point component (2-ethylhexanol), and the product yield decreases. If the temperature exceeds 160 ° C, the high boiling point component may flow sideways along with the middle boiling point component.
- the temperature of the outlet intermediate stage NR2 provided at a position where 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 within a range of 130 to 140 ° C. under a pressure of 16.671 kPa. If it is less than 130 °C low boiling point component is not easy to remove, if it exceeds 140 °C high boiling point component is not easy to have a big impact on product purity.
- the temperature range of the outflow intermediate stage (NR2) of the tower top zone, the tower bottom zone and the main tower is based on 16.671 kPa (slightly reduced at normal pressure), and the temperature range may be changed when the distillation column is operated under reduced pressure or pressure. In general, as the pressure increases, the upper limit temperature and the lower limit temperature also tend to increase.
- the temperature of the top zone may use the upper and lower temperature ranges calculated using Equation 1 below.
- T 1a And T 2a Is the temperature, the unit is °C; P is the pressure, in kPa ; 0.981 ⁇ P ⁇ 980.665, P ⁇ 16.671)
- the temperature of the bottom zone may use the upper and lower temperature ranges calculated using Equation 2 below.
- T 1b And T 2b Is the temperature, the unit is °C; P is the pressure, in kPa ; 0.981 ⁇ P ⁇ 980.665, P ⁇ 16.671)
- the temperature of the outflow intermediate stage NR2 may use the upper and lower temperature ranges calculated using Equation 3 below.
- T 1c And T 2c Is the temperature, the unit is °C; P is the pressure, in kPa ; 0.981 ⁇ P ⁇ 980.665, P ⁇ 16.671)
- the operating conditions of the dividing wall distillation column of the present invention reflecting the temperature of the tower top zone, the top bottom zone and the outflow intermediate stage according to the pressure is as follows.
- the heat-comprising distillation column having a dividing wall aims at improving the tower efficiency of a distillation system for a mixture of three or more components.
- a space that functions as a pre-separator and a main separator having a liquid composition distribution similar to the above it has the same effect as that of two distillation columns.
- the present invention relates to a 2-ethylhexanol fractional distillation method characterized in that to produce 2-ethylhexanol using the above-described 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.
- a comparative example two distillation columns without a conventional dividing wall were used, and as an example, one distillation column with a dividing wall was used.
- the content of 2-ethylhexanol in the raw materials was 96.09% by weight in both Comparative Examples and Examples.
- FIGS. 6 and 7 show Comparative Examples and Examples, respectively.
- the numbers 1 to 8 of FIGS. 6 and 7 are identification numbers representing individual streams shown in the drawings of the examples and the comparative examples, respectively.
- the Examples and Comparative Examples had the theoretical number shown in Table 1, and the length of the separation wall in the Example corresponds to 84% of the total number of theoretical words in the top, upper feed, bottom outlet and top bottom areas. Stage.
- the high purity 2-ethylhexanol of 99 wt% or more was efficiently obtained due to the removal of the remixing phenomenon and the increase in the separation efficiency.
- Increased product purity can reduce the additional step of rectification recycle of 2-ethylhexanol and increase productivity.
- DWC (1 column and 2 heat exchangers) is much cheaper than existing distillation columns (2 columns and 4 heat exchangers).
- the energy saving rate has been greatly reduced to about 34.0%.
- first tower 21 second tower
- tower top zone 200 upper feed zone
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Abstract
Description
항목 | 이론단수 | |
실시예 | 탑정 구역(100) | 13 |
상부 공급 구역(200) | 15 | |
상부 유출 구역(300) | 37 | |
하부 공급 구역(400) | 6 | |
하부 유출 구역(500) | 24 | |
탑저 구역(600) | 12 | |
비교예 | 1st column | 33 |
2nd column | 49 |
비교예 | 실시예 | 절감량(x107 KJ/hr) | 절감율(%) | |||
에너지 소비량(x107 KJ/hr) | Total | 1st column | 2nd column | 1.11 | 0.57 | 34.0 |
1.68 | 0.54 | 1.14 |
Claims (12)
- 응축기, 재비기, 및 분리벽이 구비된 주탑을 포함하는 분리벽형 증류탑에 있어서,상기 주탑은 탑정구역, 상부 공급 구역, 상부 유출 구역, 하부 공급 구역, 하부 유출 구역 및 탑저구역으로 구분되고,크루드 2-에틸헥산올 원료가 상기 상부 공급 구역 및 상기 하부 공급 구역이 접하는 공급중간단으로 유입되고, 저비점 성분은 상기 탑정구역에서 유출되고, 고비점 성분은 상기 탑저구역에서 유출되고, 중비점 성분은 상기 상부 유출 구역 및 상기 하부 유출 구역이 접하는 유출중간단으로 유출되며,상기 중비점 성분은 2-에틸헥산올인 것임을 특징으로 하는 분리벽형 증류탑.
- 제 1 항에 있어서, 상기 원료는 2-에틸헥산올 함량이 90 중량% 이상인 것임을 특징으로 하는 분리벽형 증류탑.
- 제 1 항에 있어서, 상기 탑정구역, 상기 상부 공급 구역, 상기 상부 유출 구역, 상기 하부 공급 구역, 상기 하부 유출 구역 및 상기 탑저구역에 구비되는 각각의 단수는 증류곡선에 의해 산출되어지는 이론단수의 80 내지 145 % 범위 이내인 것임을 특징으로 하는 분리벽형 증류탑.
- 제 1 항에 있어서, 상기 분리벽의 길이는 상기 상부 공급 구역 및 상기 하부 공급 구역 전체 이론단수에 따라 그 길이가 결정되어지는 것임을 특징으로 하는 분리벽형 증류탑.
- 제 1 항에 있어서, 상기 분리벽의 길이는 증류곡선에 의해 산출되어지는 상기 탑정구역, 상기 상부 공급 구역, 상기 하부 유출 구역 및 상기 탑저구역 전체 이론단수의 30 내지 85 % 범위 이내인 것임을 특징으로 하는 분리벽형 증류탑.
- 제 1 항에 있어서, 상기 탑정구역의 온도는 16.671kPa 압력하에서 75 내지 85 ℃ 범위 이내인 것임을 특징으로 하는 분리벽형 증류탑.
- 제 1 항에 있어서, 상기 탑저구역의 온도는 16.671kPa 압력하에서 145 내지 160 ℃ 범위 이내인 것임을 특징으로 하는 분리벽형 증류탑.
- 제 1 항에 있어서, 상기 상부 유출 구역 및 상기 하부 유출 구역이 접하는 위치에 구비되고 중비점 성분이 유출되는 상기 유출중간단의 온도는 16.671kPa 압력하에서 130 내지 140 ℃ 범위 이내인 것임을 특징으로 하는 분리벽형 증류탑.
- 제 1 항에 있어서, 상기 탑정구역의 온도는 압력이 16.671kPa이 아닌 경우에 하기 수학식 1을 따르는 하한온도(T1a) 내지 상한온도(T2a) 범위 이내인 것임을 특징으로 하는 분리벽형 증류탑.[수학식 1]하한: T1a = 114.5099*P0.2439상한: T2a = 123.4949*P0.2149(여기서, T1a 및 T2a는 온도로서, 단위는 ℃ ; P는 압력으로서, 단위는 kPa ; 0.981 ≤ P ≤ 980.665, P ≠ 16.671)
- 제 1 항에 있어서, 상기 탑저구역의 온도는 압력이 16.671kPa이 아닌 경우에 하기 수학식 2를 따르는 하한온도(T1b) 내지 상한온도(T2b) 범위 이내인 것임을 특징으로 하는 분리벽형 증류탑.[수학식 2]하한: T1b = 192.1386*P0.1548상한: T2b = 206.5980*P0.1405(여기서, T1b 및 T2b는 온도로서, 단위는 ℃ ; P는 압력으로서, 단위는 kPa ; 0.981 ≤ P ≤ 980.665, P ≠ 16.671)
- 제 1 항에 있어서, 상기 상부 유출 구역 및 상기 하부 유출 구역이 접하는 위치에 구비되고 중비점 성분이 유출되는 상기 유출중간단의 온도는 압력이 16.671kPa이 아닌 경우에 하기 수학식 3을 따르는 하한온도(T1c) 내지 상한온도(T2c) 범위 이내인 것임을 특징으로 하는 분리벽형 증류탑.[수학식 3]하한: T1c = 157.7845*P0.1034상한: T2c = 167.6350*P0.096(여기서, T1c 및 T2c는 온도로서, 단위는 ℃ ; P는 압력으로서, 단위는 kPa ; 0.981 ≤ P ≤ 980.665, P ≠ 16.671)
- 제1항 내지 제11항 중 어느 한 항에 따른 분리벽형 증류탑을 이용하여 2-에틸헥산올을 생산함을 특징으로 하는 2-에틸헥산올 분별증류방법.
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JP2012500728A JP5720669B2 (ja) | 2009-03-19 | 2010-03-19 | 高純度の2−エチルヘキサノール生産のための分離壁型蒸留塔及びこれを利用した分別蒸留方法 |
CN201080012285.0A CN102355928B (zh) | 2009-03-19 | 2010-03-19 | 用于制备高纯度2-乙基己醇的分隔壁蒸馏塔和采用该分隔壁蒸馏塔的分馏方法 |
EP10753733A EP2409746A4 (en) | 2009-03-19 | 2010-03-19 | DISTILLATION COLUMN WITH SEPARATION WALL FOR THE PRODUCTION OF HIGH-PURITY 2-ETHYLHEXANOL AND FRACTIONATION METHOD USING THESE COLUMNS |
US13/256,430 US8764946B2 (en) | 2009-03-19 | 2010-03-19 | Dividing wall distillation columns for production of high-purity 2-ethylhexanol and fractionation method using same |
US13/943,536 US9511306B2 (en) | 2009-03-19 | 2013-07-16 | Dividing wall distillation columns for production of high-purity 2-ethylhexanol and fractionation method using same |
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JP2014531309A (ja) * | 2011-09-19 | 2014-11-27 | エルジー・ケム・リミテッド | デュアルモード分離壁型蒸留塔 |
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JP2014508736A (ja) * | 2010-12-29 | 2014-04-10 | エルジー・ケム・リミテッド | 高純度の2−エチルヘキシル−アクリレート生産のための分離壁型蒸留塔及びこれを利用した製造方法 |
JP2014531309A (ja) * | 2011-09-19 | 2014-11-27 | エルジー・ケム・リミテッド | デュアルモード分離壁型蒸留塔 |
US10112122B2 (en) | 2013-01-16 | 2018-10-30 | Lg Chem, Ltd. | Device for preparing alkanol |
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WO2010107283A3 (ko) | 2010-12-23 |
US8764946B2 (en) | 2014-07-01 |
EP2409746A4 (en) | 2012-05-30 |
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US20120004473A1 (en) | 2012-01-05 |
JP5720669B2 (ja) | 2015-05-20 |
EP2409746A2 (en) | 2012-01-25 |
JP2012520874A (ja) | 2012-09-10 |
KR20100105500A (ko) | 2010-09-29 |
US20130334029A1 (en) | 2013-12-19 |
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US9511306B2 (en) | 2016-12-06 |
KR101191112B1 (ko) | 2012-10-15 |
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