WO2018114429A1 - Verfahren zur destillativen gewinnung von rein-2-ethylhexylacrylat oder rein-2-propylheptylacrylat aus dem entsprechenden roh-alkylacrylat - Google Patents
Verfahren zur destillativen gewinnung von rein-2-ethylhexylacrylat oder rein-2-propylheptylacrylat aus dem entsprechenden roh-alkylacrylat Download PDFInfo
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- WO2018114429A1 WO2018114429A1 PCT/EP2017/082203 EP2017082203W WO2018114429A1 WO 2018114429 A1 WO2018114429 A1 WO 2018114429A1 EP 2017082203 W EP2017082203 W EP 2017082203W WO 2018114429 A1 WO2018114429 A1 WO 2018114429A1
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- acrylate
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- separation stage
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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
-
- 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
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
- B01D3/22—Fractionating columns in which vapour bubbles through liquid with horizontal sieve plates or grids; Construction of sieve plates or grids
- B01D3/225—Dual-flow sieve trays
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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
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
- B01D3/4283—Bottom stream
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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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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C69/00—Esters of carboxylic acids; Esters of carbonic or haloformic acids
- C07C69/52—Esters of acyclic unsaturated carboxylic acids having the esterified carboxyl group bound to an acyclic carbon atom
- C07C69/533—Monocarboxylic acid esters having only one carbon-to-carbon double bond
- C07C69/54—Acrylic acid esters; Methacrylic acid esters
Definitions
- R is an alkyl radical.
- Acrylates such as, for example, 2-ethylhexyl acrylate and 2-propylheptyl acrylate are generally obtained industrially by reacting alcohol (for example 2-ethylhexanol or 2-propylheptanol) and acrylic acid.
- alcohol for example 2-ethylhexanol or 2-propylheptanol
- acrylic acid for example 2-ethylhexanol or 2-propylheptanol
- a product mixture is formed, also called crude acrylate, in which the acrylate generally predominates.
- R thus corresponds to 2-ethylhexyl and 2-propylheptyl.
- Alkyl acrylates are used for paints, adhesives, construction chemicals, paper coatings and plastics.
- the crude acrylate obtained in a synthesis must be further purified by distillation.
- distillative recovery of acrylate from crude acrylate is carried out after a preferred pre-cleaning, e.g. by extraction, in the art, e.g. in the thesis "Polymerization inhibition of (meth) acrylates", TU Darmstadt (Department of Chemistry), 2003, by Holger Becker on pages 21 to 24 is shown, in two series-connected distillation columns:
- ROH alcohol
- ROR diether
- the higher boilers based on the 2-ethylhexyl acrylate or 2-propylheptyl acrylate
- 2-ethylhexyloxy ester or 2-propylheptyloxy ester (ROCH 2 CH 2 C (0O) OR)
- the desired product ie pure 2-ethylhexyl acrylate or pure 2-propylheptyl acrylate
- the bottom effluent of column I is fed to a high-boiling precipitator J (see Fig. 3-7 on page 24 of the above-mentioned thesis).
- the object of the invention was to provide an improved process for the distillative recovery of pure 2-ethylhexyl acrylate or pure 2-propylheptyl acrylate from the respective corresponding crude alkyl acrylate, which, while maintaining the respective required specifications for the Pure 2-ethylhexyl acrylate and pure 2-propylheptyl acrylate, is more economical, especially with regard to investment and energy costs.
- a process for the recovery by distillation of pure 2-ethylhexyl acrylate or pure 2-propylheptyl acrylate from the corresponding crude alkyl acrylate is found, which is characterized in that the method in a dividing wall column (1) with separating internals and evaporator (7) in which a partition wall (8) in the column longitudinal direction to form an upper common column region (9), a lower common column region (14), a feed part (10, 12) with a side feed parts (2) and a removal part (1 1, 13 ) with a side removal part (3), the column has a number of theoretical plates in the range of 10 to 60, the side feed parts (2) for the corresponding crude alkyl acrylate on a theoretical plate in the range starting at least two theoretical plates above the lowest and ending at least two theoretical plates below the highest theoretical Separation stage is arranged, the side removal parts (3) for the pure 2-ethylhexyl acrylate or pure 2-propylheptyl on a theoretical separation stage in the range beginning at
- Under crude alkyl acrylate is especially a mixture having an acrylate content of in each case> 40 wt .-% to ⁇ 99 wt .-%, in particular> 60 wt .-% to ⁇ 98 wt .-%, 2-ethylhexyl acrylate or 2 -Propylheptylacrylat to understand.
- the crude 2-ethylhexyl acrylate used in the process according to the invention has in particular the following composition:
- the crude 2-propylheptyl acrylate used in the process according to the invention has in particular the following composition:
- the process according to the invention is carried out in a dividing wall column (1) in which a dividing wall (8) in the longitudinal direction of the column forms an upper common column region (9), a lower common column region (14), an inlet part (10, 12) and a Removal part (1 1, 13) is arranged.
- a dividing wall column is a distillation column with a vertical dividing wall, which prevents cross-mixing of liquid and vapor streams in some areas.
- the partition which usually consists of a flat sheet metal and can be welded, screwed or plugged, divides the column in the longitudinal direction in the central region into an inlet part and a removal part.
- the mixture to be separated, the corresponding crude alkyl acrylate is fed to the feed section and the product, the pure 2-ethylhexyl acrylate or, correspondingly, pure 2-propylheptyl acrylate, is withdrawn from the withdrawal section.
- the process is preferably carried out continuously.
- the dividing wall column is, as usually each distillation column, equipped with an evaporator (bottom evaporator) (7) and a condenser (6) at the top of the column.
- the residence time in the evaporator (7) and the associated piping system is advantageously limited to 1 to 60 minutes, more preferably 10 to 30 minutes.
- the liquid quantity ratio at the upper end of the dividing wall (8) on the reinforcing member (10) and the stripping section (1 1) of the column ie quantity on reinforcing member (10): quantity on stripping section (1 1), in one area from 1: 0.2 to 1: 5, ie 5 to 0.2, preferably in a range of 1: 0.5 to 1: 2, that is 2 to 0.5 set.
- This is preferably done in such a way that the liquid is collected at the upper end of the partition and fed via a control or adjusting device in said ratio to the gain or stripping section of the column. This ensures lower energy consumption.
- the amounts of the vapor streams are transferred to the stripping section (12) and the reinforcing section (13) of the column, that is to say to the stripping section (12): Amount on reinforcing member (13), in a ratio in the range of 1: 0.5 to 1: 2.0, ie 2 to 0.5, preferably in a ratio in the range of 1: 0.9 to 1: 1, 5 , ie 1 / 0.9 to 1/1, 5, set.
- the process according to the invention is preferably carried out at a pressure in the column head of from 10 mbar to 5 bar, preferably from 10 to 100 mbar.
- a temperature control is provided in the upper common column region (9), with a temperature signal, which may be from a single or averaged by several measuring points below the top theoretical separation stage, preferably counted from the top of the third theoretical separation stage, the distillate as a control variable , the reflux ratio or, preferably, the amount of return uses.
- a temperature control is provided in the lower column region, with a temperature signal which can come from a single or averaged of several measuring points above the lowest theoretical separation stage, preferably counted from below on the second theoretical separation stage, as the manipulated variable uses the sump withdrawal amount.
- a level control at the bottom of the column, which uses the page removal amount as a manipulated variable.
- the ratio of the cross-sectional areas of the region of the extraction part (11, 13) to the region of the inlet part (10, 12) is preferably 4: 1 to 1: 4, more preferably 1: 5: 1 to 1: 1, 5, e.g. at 1: 1.
- the dividing wall column (1) has a number of theoretical plates in the range of 10 to 60.
- Separating internals are located in the common upper column area (9) and in the common lower column area (14) and in the inlet part (10, 12) and removal part (1 1, 13).
- the indication of the number of theoretical plates of the dividing wall column (1) always refers to the sum of the theoretical plates in the common upper column region (9), the common lower column region (14) and the inlet part (10, 12).
- the number of theoretical plates in the extraction part (1 1, 13) is the same size as in the inlet part (10, 12), but can also be larger, for example, 1 to 5 larger, or smaller, for example, 1 to 5 smaller, be.
- the side feed parts (2) for the corresponding crude alkyl acrylate is on a theoretical separation stage in the range beginning at least two theoretical plates above the lowest and ending at least two theoretical plates below the top theoretical plate, preferably on a theoretical plate in the range beginning at least four theoretical plates above the lowest and ending at least four theoretical see separation stages below the top theoretical separation stage arranged.
- the side removal parts (3) for the pure 2-ethylhexyl acrylate or pure 2-propylheptyl acrylate is on a theoretical separation stage in the range starting at least two theoretical plates above the lowest and ending at least two theoretical plates below the top theoretical plate, preferably in the range starting at least four theoretical plates above the lowest and ending at least four theoretical plates below the top theoretical plate.
- the dividing wall (8) is in the column in the range starting at least one theoretical separation stage above the lowest and ending at least one theoretical separation stage below the top theoretical separation stage, preferably in the range beginning at least two theoretical separation stages above the lowest and ending at least two theoretical separation stages below top theoretical separation stage, particularly preferably in the middle, arranged.
- the dividing wall column (1) has a number of theoretical plates in the range of 15 to 30, the side feed parts (2) for the corresponding crude alkyl acrylate is on a theoretical separation stage in the range starting at least eight theoretical plates above the lowest and terminating at least six theoretical plates below the topmost theoretical plate, the side-siphon parts (3) for the pure 2-ethylhexyl acrylate or pure 2-propylheptyl acrylate being at a theoretical plate in the range starting at least five theoretical
- Separating stages above the lowest and ending at least eight theoretical plates arranged below the uppermost theoretical separation stage and the dividing wall (8) in the column is arranged in the range beginning at least three theoretical plates above the lowest and ending at least three theoretical plates below the top theoretical plate.
- the side removal parts (3) both on the same theoretical separation stage as the side inlet parts (2) and below or above the side inlet parts lie; but of course each on the other side of the partition (8) (see Figure 1);
- the opposing side removal parts (3) are below, for example one to 25, especially 5 to 20, especially 6 to 15, theoretical plates below, the side inlet parts (2). (The counting of the separation stages takes place in the column or in the relevant column area or in the relevant column part always from bottom to top).
- dual-flow trays are used as separating internals in the dividing wall column.
- the term dual-flow tray denotes in a known manner a column bottom with openings that are passed by vapor and liquid in the counterflow.
- Mixtures that can be subjected to thermal treatment in a column are typically fluid, i. gaseous, liquid or gaseous / liquid.
- Dual-flow trays are preferably used in the region of the dividing wall (10, 11, 12, 13); In a further preferred embodiment, dual-flow trays are also used in the common upper column region (9) and in the common lower column region (14).
- a further advantageous embodiment is the use of dual-flow trays in the region of the dividing wall (10, 11, 12, 13) and in the common lower column region (14) as well as the use of random packings or packings in the common upper column region (9).
- WO 03/043712 A1 BASF AG it was shown for a conventional column without a partition wall that a targeted reduction of the diameter of the openings in the dual-flow trays achieves a considerable reduction in susceptibility to soiling and thus a considerable extension of the operating time of tray columns could be.
- the targeted design of the opening conditions, the gas distribution to the inlet side and the sampling side can be accurately adjusted. Due to the different opening ratios of the dual-flow trays, different amounts of gas are produced on both sides of the dividing wall with the same pressure loss. This can be dispensed with a complex gas distribution below the partition.
- the opening ratio is set by the size and / or number of openings.
- the ratio of the sum of the opening areas and the total area of the dual-flow floor is designated in a known manner as the opening ratio of a dual-flow tray.
- the openings of the dual-flow trays within a column can be designed differently, specifically in such a way that the diameter of the openings and / or the number of openings are varied.
- the openings in the dual-flow trays are circular.
- the skilled person can easily determine the required opening ratio depending on the gas and liquid load and the opening diameter.
- the diameter of the openings in the dual-flow trays is preferably in the range of 10 to 80 mm, wherein above the inlet arranged dual-flow trays preferably openings in the range of 10 to 50 mm, arranged below the inlet dual-flow trays on the other hand preferably have openings with diameters in the range of 15 to 80 mm.
- the opening ratio of the dual-flow trays is preferably in the range of 10 to 30%.
- the acrylic monomer ie the 2-ethylhexyl acrylate and 2-propylheptyl acrylate
- suitable polymerization inhibitors in order to obtain a to avoid unwanted polymerization. That is, the process according to the invention is preferably carried out in the presence of effective amounts of one or more stabilizers.
- Suitable stabilizers are in principle all polymerization inhibitors which are recommended for stabilizing (meth) acrylic acid and (meth) acrylic esters in, for example, DE 10 2005 053 982 A1 (BASF AG) and DE 102 58 329 A1 (BASF AG).
- Suitable stabilizers can be, for example, N-oxides (nitroxyl or N-oxyl radicals, ie compounds which have at least one> N-0 group), such as, for example, 4-hydroxy-2,2,6,6-tetra- methylpiperidine-N-oxyl or 4-oxo-2,2,6,6-tetramethylpiperidine-N-oxyl, phenols and naphthols such as p-methoxyphenol, p-aminophenol , p-nitrosophenol, 2-tert-butylphenol, 4-tert-butylphenol, 2,4-di-tert-butylphenol, 2-methyl-4-tert-butylphenol, 2,6-tert-butyl 4-methylphenol or 4-tert-butyl-2,6-dimethylphenol, quinones, such as Hydroquinone or hydroquinone monomethyl ether, aromatic amines, e.g.
- ⁇ , ⁇ -diphenylamine phenylenediamines, e.g. N, N'-dialkyl-p-phenylenediamine, wherein the alkyl radicals may be the same or different and each independently have 1 to 4 carbon atoms and may be straight-chain or branched, such as e.g. N, N'-dimethyl-p-phenylenediamine or N, N'-diethyl-p-phenylenediamine, hydroxylamines, e.g. ⁇ , ⁇ -diethylhydroxylamine, imines, e.g. Methyl ethyl imine or methylene violet, sulfonamides, e.g.
- N-methyl-4-toluenesulfonamide or N-tert-butyl-4-toluenesulfonamide oximes, such as aldoximes, ketoximes or amidoximes, such as e.g. Diethylketoxime, methylethylketoxime or salicylaldoxime, phosphorus-containing compounds, such as e.g. Triphenylphosphine, triphenyl phosphite or triethyl phosphite, sulfur containing compounds such as e.g. Diphenyl sulfide or phenothiazine, metal salts, e.g. Cerium (III) acetate or cerium (III) ethylhexanoate, or mixtures thereof.
- oximes such as aldoximes, ketoximes or amidoximes, such as e.g. Diethylketoxime, methylethylketoxime or salicylaldoxime
- the stabilization is preferably carried out with phenothiazine (PTZ), p-methoxyphenol (MeHQ), hydroquinone, hydroquinone monomethyl ether, 4-hydroxy-2,2,6,6-tetramethylpiperidine-N-oxyl, 4-oxo-2,2,6,6 tetramethylpiperidine-N-oxyl, 2,6-tert-butyl-4-methylphenol or mixtures thereof.
- phenothiazine (PTZ) and / or p-methoxyphenol (MeHQ) as the polymerization inhibitor.
- the inhibitors can be added as pure substance, it is advantageous to add the inhibitor dissolved in a solvent as a solution which can be dosed in a simple and reproducible manner, inhibitor mixtures in principle also being possible in a single solution.
- a liquid already present in the acrylate synthesis process or the mixture of substances in the column is used as the solvent.
- Particularly preferred for the choice as solvent is the acrylate product itself (here 2-ethylhexyl or 2-propylheptyl acrylate) or one of the synthetic starting materials for the acrylate (in this case acrylic acid or 2-ethylhexanol or 2-propylheptanol).
- the drawing shows in the single figure a dividing wall column 1 with a partition wall 8, the dividing wall column 1 in a common upper column area 9, an inlet part 10 and 12, with reinforcing member 10 and output member 12, a removal part 1 1 and 13 with a stripping section 1 1 and a reinforcing part 13, as well as a common lower column region 14.
- Separating internals are in the column areas 9 and 14 and in the parts 10 to 13.
- the corresponding crude alkyl acrylate 2 occurs between the column parts 10 and 12 in the dividing wall column 1 a.
- the pure 2-ethylhexyl acrylate or, correspondingly, pure 2-propylheptyl acrylate, 3, is taken off between column parts 11 and 13, preferably in liquid form.
- the vapor stream 15 produced at the top of the column is partially condensed in the condenser 6, which is optionally supplemented by an aftercooler, and divided into the reflux stream 16 and the distillate stream 4.
- the non-condensed portion from the condenser 6 contains the low-boiling impurities and is withdrawn in vapor form as stream 19.
- the liquid 17 is partially vaporized in an evaporator 7 and returned via the pipe 18 into the column.
- a partial stream 5 containing the higher-boiling impurities is withdrawn.
- the evaporator 7 may be designed as a natural circulation evaporator or as a forced circulation evaporator, in the latter case, a circulation pump for the liquid flow 17 is additionally required. It is particularly advantageous with regard to avoiding unwanted polymerization reactions to use a falling-film evaporator instead of the forced-circulation evaporator, since the shortest residence times are possible with this design. To reduce the residence time of the liquid in the evaporator system, it is advantageous not to position the posture in the lower column hood, but in the feed line of the liquid 17.
- a stabilizer 1 (23) (so-called process stabilizer, eg PTZ in particular) in the reinforcement part (10) of the inlet part (10, 12), there in particular just below the upper end of the partition wall (8) is added.
- the stabilizer 1 may in particular be used as a solution in a suitable solvent, especially as listed above, e.g. 2-ethylhexyl acrylate or 2-propylheptyl acrylate, are used.
- a suitable solvent especially as listed above, e.g. 2-ethylhexyl acrylate or 2-propylheptyl acrylate
- a stabilizer 2 (22) (so-called storage stabilizer, for example MeHQ in particular) is preferably introduced into the container (20) which collects the condensate (26) and / or into the conduit of a quench circuit (21) and / or at the top of the condenser (6).
- the preferably configured quench circuit ie the liquid recycle stream of a portion of the condensate, eg 10 to 50 weight percent of the condensate, into the Capacitor (6)
- the preferably configured quench circuit ie the liquid recycle stream of a portion of the condensate, eg 10 to 50 weight percent of the condensate, into the Capacitor (6)
- the preferably configured quench circuit ie the liquid recycle stream of a portion of the condensate, eg 10 to 50 weight percent of the condensate, into the Capacitor (6)
- the supply of lean air (25) (mixture of air and nitrogen, in particular such that an oxygen content of 4 to 9 vol.% Results) occurs particularly either at the lower end of the evaporator (7) or at the lower end of the column (1).
- process stabilizer (24), in particular PTZ, is additionally added to the reinforcing part (13) below the side removal parts (3).
- a "low boiler” (based on the relevant alkyl acrylate) is a substance whose boiling point is lower than the boiling point of the alkyl acrylate in question, ie 2-ethylhexyl acrylate or 2-propylheptyl acrylate, at the same pressure.
- a 'high boiler' (based on the relevant alkyl acrylate) is a substance whose boiling point is higher than the boiling point of the relevant alkyl acrylate, ie 2-ethylhexyl acrylate or 2-propylheptyl acrylate, at the same pressure.
- the operating modes are presented on the basis of data from a thermodynamic simulation of an overall plant for the production of 2-ethylhexyl acrylate.
- thermodynamic simulation of the process was performed with the software Aspen Plus® (short: Aspen).
- Aspen is a comprehensive simulation software used to model, simulate, and optimize chemical processes and equipment in the industry.
- Aspen has extensive model databases to model the basic operations as well as substance databases for the material properties of many different substances.
- the properties of mixtures are calculated by Aspen using different thermodynamic models from the substance data of pure substances.
- a crude 2-ethylhexyl acrylate stream of 19180 kg / h with a temperature of 145 ° C was liquid fed to the 14th theoretical separation stage of a dividing wall column (1) with a total of 22 theoretical plates.
- the crude 2-ethylhexyl acrylate had the following composition:
- the side trigger (3) had the following composition:
- the distillation yield for 2-ethylhexyl acrylate was over 93%.
- At the lower end of the partition wall (8) was the division of the vapor flow amounts, stripping section (12): reinforcing member (13), in the ratio 1: 1.
- the heating capacity of the evaporator was 2175 kW.
- a crude 2-ethylhexyl acrylate stream of 19180 kg / h with a temperature of 145 ° C was liquid fed to the 14th theoretical separation stage of a dividing wall column (1) with a total of 22 theoretical plates.
- the crude 2-ethylhexyl acrylate had the following composition:
- the side trigger (3) had the following composition:
- a crude 2-ethylhexyl acrylate stream of 19180 kg / h at a temperature of 145 ° C was liquid at the 14th theoretical separation stage of a dividing wall column (1) with a total of 22 theoretical see stages fed.
- the crude 2-ethylhexyl acrylate had the following composition:
- the side trigger (3) had the following composition:
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
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Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1020197021008A KR102519257B1 (ko) | 2016-12-21 | 2017-12-11 | 순수 2-에틸헥실 아크릴레이트 또는 순수 2-프로필헵틸 아크릴레이트를 상응하는 조질 알킬 아크릴레이트로부터 증류에 의해 단리하는 방법 |
EP17832205.3A EP3558923B1 (de) | 2016-12-21 | 2017-12-11 | Verfahren zur destillativen gewinnung von rein-2-ethylhexylacrylat oder rein-2-propylheptylacrylat aus dem entsprechenden roh-alkylacrylat |
JP2019533475A JP7337692B2 (ja) | 2016-12-21 | 2017-12-11 | 蒸留により対応する粗製アルキルアクリレートから純粋な2-エチルヘキシルアクリレートまたは純粋な2-プロピルヘプチルアクリレートを取得する方法 |
MYPI2019003485A MY193152A (en) | 2016-12-21 | 2017-12-11 | Process for isolating pure 2-ethylhexyl acrylate or pure 2-propylheptyl acrylate from the corresponding crude alkyl acrylate by distillation |
CN201780079912.4A CN110099891B (zh) | 2016-12-21 | 2017-12-11 | 通过蒸馏将纯丙烯酸2-乙基己酯或纯丙烯酸2-丙基庚酯从相应的粗丙烯酸烷基酯中分离的方法 |
BR112019011301-0A BR112019011301B1 (pt) | 2016-12-21 | 2017-12-11 | Processo para isolar acrilato de 2-etil-hexila puro ou acrilato de 2-propil-heptila puro do acrilato de alquila bruto. |
US16/472,054 US10894223B2 (en) | 2016-12-21 | 2017-12-11 | Process for isolating pure 2-ethylhexyl acrylate or pure 2-propylheptyl acrylate from the corresponding crude alkyl acrylate by distillation |
ZA2019/04648A ZA201904648B (en) | 2016-12-21 | 2019-07-16 | Method for obtaining pure 2-ethylhexyl acrylate or pure 2-propylheptyl acrylate from the corresponding raw alkyl acrylate by distillation |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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EP16205968.7 | 2016-12-21 | ||
EP16205968 | 2016-12-21 |
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WO2018114429A1 true WO2018114429A1 (de) | 2018-06-28 |
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PCT/EP2017/082203 WO2018114429A1 (de) | 2016-12-21 | 2017-12-11 | Verfahren zur destillativen gewinnung von rein-2-ethylhexylacrylat oder rein-2-propylheptylacrylat aus dem entsprechenden roh-alkylacrylat |
Country Status (10)
Country | Link |
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US (1) | US10894223B2 (de) |
EP (1) | EP3558923B1 (de) |
JP (1) | JP7337692B2 (de) |
KR (1) | KR102519257B1 (de) |
CN (1) | CN110099891B (de) |
BR (1) | BR112019011301B1 (de) |
MY (1) | MY193152A (de) |
TW (1) | TWI778001B (de) |
WO (1) | WO2018114429A1 (de) |
ZA (1) | ZA201904648B (de) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3091871A1 (fr) | 2019-01-22 | 2020-07-24 | Arkema France | Procede de purification d’esters (meth)acryliques a l’aide d’une colonne a partition |
WO2020234519A1 (fr) | 2019-05-23 | 2020-11-26 | Arkema France | Procede perfectionne de fabrication d'acrylates d'alkyle de purete elevee |
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KR102670910B1 (ko) * | 2021-03-16 | 2024-05-29 | 한화솔루션 주식회사 | 증발기 및 이를 이용한 분리 방법 |
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DE3302525A1 (de) | 1983-01-26 | 1984-07-26 | Basf Ag, 6700 Ludwigshafen | Destillationskolonne zur destillativen zerlegung eines aus mehreren fraktionen bestehenden zulaufproduktes |
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FR3091871A1 (fr) | 2019-01-22 | 2020-07-24 | Arkema France | Procede de purification d’esters (meth)acryliques a l’aide d’une colonne a partition |
WO2020152415A1 (fr) | 2019-01-22 | 2020-07-30 | Arkema France | Procede de purification d'esters (meth)acryliques a l'aide d'une colonne a partition |
CN113348162A (zh) * | 2019-01-22 | 2021-09-03 | 阿科玛法国公司 | 使用分壁式塔来纯化(甲基)丙烯酸酯的方法 |
KR20210116596A (ko) * | 2019-01-22 | 2021-09-27 | 아르끄마 프랑스 | 분리 벽 컬럼을 사용하여 (메트)아크릴산 에스테르를 정제하기 위한 방법 |
KR102362742B1 (ko) | 2019-01-22 | 2022-02-14 | 아르끄마 프랑스 | 분리 벽 컬럼을 사용하여 (메트)아크릴산 에스테르를 정제하기 위한 방법 |
WO2020234519A1 (fr) | 2019-05-23 | 2020-11-26 | Arkema France | Procede perfectionne de fabrication d'acrylates d'alkyle de purete elevee |
FR3096368A1 (fr) | 2019-05-23 | 2020-11-27 | Arkema France | Procede perfectionne de fabrication d’acrylates d’alkyle de purete elevee |
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JP2020502212A (ja) | 2020-01-23 |
BR112019011301A2 (pt) | 2019-10-08 |
JP7337692B2 (ja) | 2023-09-04 |
KR20190098198A (ko) | 2019-08-21 |
EP3558923A1 (de) | 2019-10-30 |
EP3558923B1 (de) | 2020-12-02 |
US20200094160A1 (en) | 2020-03-26 |
CN110099891A (zh) | 2019-08-06 |
BR112019011301B1 (pt) | 2022-11-29 |
TWI778001B (zh) | 2022-09-21 |
ZA201904648B (en) | 2024-03-27 |
TW201835027A (zh) | 2018-10-01 |
MY193152A (en) | 2022-09-26 |
US10894223B2 (en) | 2021-01-19 |
CN110099891B (zh) | 2022-06-10 |
KR102519257B1 (ko) | 2023-04-07 |
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