WO1995017937A1 - Verfahren zum aufarbeiten eines reaktioinsgemischs mittels einer auf den reaktor aufgesetzten kolonne - Google Patents
Verfahren zum aufarbeiten eines reaktioinsgemischs mittels einer auf den reaktor aufgesetzten kolonne Download PDFInfo
- Publication number
- WO1995017937A1 WO1995017937A1 PCT/EP1994/004170 EP9404170W WO9517937A1 WO 1995017937 A1 WO1995017937 A1 WO 1995017937A1 EP 9404170 W EP9404170 W EP 9404170W WO 9517937 A1 WO9517937 A1 WO 9517937A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- column
- reaction
- product
- mixture
- working
- Prior art date
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1868—Stationary reactors having moving elements inside resulting in a loop-type movement
- B01J19/1881—Stationary reactors having moving elements inside resulting in a loop-type movement externally, i.e. the mixture leaving the vessel and subsequently re-entering it
-
- 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
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
-
- 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
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
-
- 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
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00162—Controlling or regulating processes controlling the pressure
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
-
- 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 invention relates to a process for working up a reaction mixture which contains high boilers as undesired by-products, low-boiling starting materials and in particular also catalyst residues, to give a valuable product of high purity, the boiling point of which lies between the boiling points of the high and low boilers.
- the product of value can be a pure substance or a mixture of isomers.
- the reaction mixture is rectified in a column placed on the reactor.
- the components of the reaction mixture with boiling points below the boiling point of the desired product of value are referred to as high boilers and the components with higher boiling points as low boilers.
- the work-up method according to the invention is not restricted to specific reaction mixtures. However, it relates in particular to reaction mixtures which are produced in the manufacture of fragrances. After processing, these must be olfactory, especially pure, which means that they must not show any odors due to by-products. Since some by-products are disruptive even in the pp range, particularly high demands have to be made of the processing method.
- the work-up process according to the invention relates to reaction mixtures which are obtained in the production of fragrances by transesterification or esterification. Examples of this can be found in S. Arctander: "Perfume and Flavor Chemicals" (Aroma Chemicals) I, published 1969, Montclair, NJ (US) No.
- the reaction is usually carried out batchwise and the water of reaction formed during the esterification or the lower alcohol released during the transesterification is withdrawn in gaseous form from the reaction space.
- the gaseous by-product and part of the starting materials are condensed in a partial condenser or a condenser and, in the event of the partial or complete insolubility of the substances, separated and further processed via a separator.
- the separated starting materials preferably go back into the reaction space.
- a column with internals can be arranged upstream of the condenser or the partial condenser, which may consist of an ordered packing, an ordered or disordered bed and also of trays.
- the crude product in the reactor is washed in order to separate catalyst residues and by-products. Neutral washing often takes place, that is to say with a basic or acidic medium, especially water instead.
- the remaining crude product contains small amounts (in the percentage range) of excess educts and other more volatile substances and less volatile by-products as well as catalyst residues.
- a discontinuous, fractional distillation is carried out, in which the more volatile substances are drawn off as a forerun.
- the main run contains the value product.
- the invention has for its object to provide an economical method of the type mentioned that provides a valuable product with high purity, washing the raw product with the resulting problems in the disposal of the washing liquid and the processing time is reduced.
- this object is achieved by continuously separating a mixture of the low boilers and the product of value from the reaction mixture in the first column placed on the reactor, the high boilers and, if appropriate, the catalyst residues remaining in the reactor , and the separated mixture is rectified in a second column which is spatially separated from the reactor and the attached column.
- the workup is carried out in two stages. In the first stage, a mixture of low boilers and the product of value is separated from the reaction mixture, which then essentially still contains the high boilers and catalyst residues. In the second stage, rectification is carried out once more and the product of value is purified from the low boilers.
- Both work-up stages can be decoupled in time if the mixture of low boilers and the product of value separated from the reaction mixture is first allowed to flow into an intermediate receiver, from which it is then fed into the second column.
- the second processing stage can be carried out independently of the first processing stage. For example, you can wait until the a sufficient amount of mixture of low boilers and valuable products was obtained in order to separate it in a particularly economical manner in the second column.
- the second work-up stage can be carried out particularly quickly and economically if the working pressure for the second column is lower than the pressure of the feed consisting of low boilers and valuable material, so that at least some of the low boilers enter the column when the feed enters evaporated spontaneously. The further concentration of the valuable substance then takes place in the column internals.
- the valuable substance which is only evaporated to a small extent, is highly enriched.
- the bottom of the column can also be heated so that the remaining low boilers evaporate.
- the valuable substance is then continuously withdrawn from the sump in high purity.
- the low boilers obtained are continuously condensed and drawn off at the top of the column.
- the process is particularly suitable for working up reaction mixtures obtained from esterification reactions or transesterification reactions.
- the production of alkyl fatty acid esters, in particular isopropyl yristat, may be mentioned as a preferred application.
- the work-up process according to the invention is also preferably used for working up the product of value salicylate ester, in particular benzyl salicylate, cyclohexyl salicylate, hexyl salicylate or isoamyl salicylate.
- salicylate ester in particular benzyl salicylate, cyclohexyl salicylate, hexyl salicylate or isoamyl salicylate.
- These are basic, homogeneously catalyzed transesterifications, in which residues of alcohol and catalyst residues in the form of soaps remain in the reaction mixture, which must be removed.
- a catalysis gates are typically sodium alcoholates, e.g. B. sodium ethylate inserted.
- washing the raw product to remove unwanted components is no longer necessary. There are no problems with washing liquids to be disposed of.
- Another particular advantage of the method according to the invention is the reduced production time. Washing times, cooling and cooling phases as well as additional intermediate cleaning of the systems are eliminated.
- FIG. 1 An exemplary embodiment of the method according to the invention is explained in more detail below on the basis of a flow diagram (FIG. 1).
- the temperature is increased and / or the pressure is reduced and part of the reaction mixture is evaporated.
- the mixture condensed on the cooler 4 is collected in a first receiver 5, partially recycled and partially fed directly or via a second receiver 6 and a heater 7 into a second rectification column 8.
- the first template 5 is used for spatial and the second template 6 for decoupling the two workup steps.
- the second template preferably has a sufficiently large capacity for an entire batch cycle. In this case, the workup in the second stage can be carried out simultaneously with the next reaction cycle in the first stage.
- the heated mixture is pumped continuously under pressure into the second rectification column 8 and partially evaporates when it enters the column. In this way, a first enrichment of the value Reached. Further enrichment takes place in the internals of column 8.
- the product of value can be drawn off at the bottom of the column and the low boilers can be drawn off at the top.
- a sump heater 9 is provided to improve the separation.
- the low boilers are condensed at the top of the column, passed into a third receiver 10, partly returned as reflux and partly drawn off.
- a mixture of the following composition is present in the reactor (1): 0.8% methyl salicylate, 2.1% benzyl alcohol and 96.7% benzyl salicylate. The concentrations indicated were determined by gas chromatography.
- the mixture of reactants and benzyl salicylate through the first rectification column (3) is lled abdest.
- the temperature at the top of the column is 173 ° C. and the pressure is 3 mbar. From the first receiver (5), 75% of the condensate obtained after the cooler (4) is added to the second receiver (6) and the remaining 25% is returned to the first rectification column (3).
- the mixture is pumped from the second receiver (6) into the heater (7). It enters the second rectification column (8) at a temperature of 120 ° C. At a bottom temperature of 173 ° C. and a pressure of 9 mbar, low boilers (in this case the benzyl alcohol and the methyl salicylate) are completely evaporated in the bottom heater (9); the sump contains olfactory pure benzyl salicylate, which has a minimum concentration of 98%.
- the distillate enriched with low boilers is obtained in the third receiver (10); the head pressure is 1 mbar and the temperature is 118 ° C. From the third template (10) 83% are returned to the second column (8) and 17% are drawn off.
- the distillate drawn off typically has a composition which has 12% benzyl alcohol, 5% methyl salicylate and 77% benzyl salicylate. The remaining constituents are volatile by-products in total.
- a mixture of the following composition is present in the reactor (1): 1.4% methyl salicylate, 4% cyclohexanol and 94.2% cyclohexyl salicylate.
- concentrations indicated were determined by gas chromatography.
- the mixture of starting materials and cyclohexylsalylate is distilled off via the first rectification column (3).
- the temperature at the top of the column is 149 ° C. and the pressure is 3 mbar.
- 75% of the condensate obtained after the cooler (4) is added to the second receiver (6) and the remaining 25% is returned to the first rectification column (3).
- the mixture is pumped from the second receiver (6) into the heater (7). It enters the second rectification column (8) at a temperature of 120 ° C. At a bottom temperature of 156 ° C. and a pressure of 8 mbar, low boilers (in this case cyclohexanol and methyl salicylate) are completely evaporated in the bottom heater (9); the sump contains olfactory pure cyclohexyl salicylate, which has a minimum concentration of 98%.
- the distillate enriched with low boilers is obtained in the third receiver (10); the head pressure is 1 mbar and the temperature 100 ° C. From the third receiver (10) 83% are moved back into the second column (8) and 17% are withdrawn.
- the stripped distillate typically has a composition comprising 24% cyclohexanol, 8% methyl salicylate and 64% cyclohexyl salicylate. The remaining constituents are volatile by-products in total.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP7517749A JPH09502735A (ja) | 1993-12-24 | 1994-12-15 | 反応器に配置したカラムにより反応混合物を処理する方法 |
EP95903805A EP0735911A1 (de) | 1993-12-24 | 1994-12-15 | Verfahren zum aufarbeiten eines reaktioinsgemischs mittels einer auf den reaktor aufgesetzten kolonne |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE4344358A DE4344358A1 (de) | 1993-12-24 | 1993-12-24 | Verfahren zum Aufarbeiten eines Reaktionsgemischs mittels einer auf den Reaktor aufgesetzen Kolonne |
DEP4344358.3 | 1993-12-24 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1995017937A1 true WO1995017937A1 (de) | 1995-07-06 |
Family
ID=6506126
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1994/004170 WO1995017937A1 (de) | 1993-12-24 | 1994-12-15 | Verfahren zum aufarbeiten eines reaktioinsgemischs mittels einer auf den reaktor aufgesetzten kolonne |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP0735911A1 (de) |
JP (1) | JPH09502735A (de) |
DE (1) | DE4344358A1 (de) |
WO (1) | WO1995017937A1 (de) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8765217B2 (en) | 2008-11-04 | 2014-07-01 | Entrotech, Inc. | Method for continuous production of (meth)acrylate syrup and adhesives therefrom |
US8329079B2 (en) | 2009-04-20 | 2012-12-11 | Entrochem, Inc. | Method and apparatus for continuous production of partially polymerized compositions and polymers therefrom |
KR101425650B1 (ko) * | 2013-03-26 | 2014-08-01 | 동아대학교 산학협력단 | 분리벽형 증류탑을 이용한 해상 액화천연가스 분별증류장치 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB246526A (en) * | 1925-01-26 | 1927-04-26 | Us Ind Alcohol Co | Process of esterification |
WO1985003084A1 (en) * | 1984-01-07 | 1985-07-18 | Henkel Kommanditgesellschaft Auf Aktien | Utilization of salicylic acid esters as perfuming substances, perfuming compositions containing them and new salicylic acid esters |
EP0280471A1 (de) * | 1987-02-23 | 1988-08-31 | BP Chemicals Limited | Verfahren zur kontinuierlichen Herstellung von Acetaten |
EP0304757A1 (de) * | 1987-08-25 | 1989-03-01 | BASF Aktiengesellschaft | Verfahren zur Herstellung von Carbonsäureestern |
WO1991019559A1 (de) * | 1990-06-15 | 1991-12-26 | Henkel Kommanditgesellschaft Auf Aktien | Verfahren zum durchführen einer gleichgewichtsreaktion unter anwendung von dämpfepermeation |
-
1993
- 1993-12-24 DE DE4344358A patent/DE4344358A1/de not_active Withdrawn
-
1994
- 1994-12-15 EP EP95903805A patent/EP0735911A1/de not_active Withdrawn
- 1994-12-15 JP JP7517749A patent/JPH09502735A/ja active Pending
- 1994-12-15 WO PCT/EP1994/004170 patent/WO1995017937A1/de not_active Application Discontinuation
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB246526A (en) * | 1925-01-26 | 1927-04-26 | Us Ind Alcohol Co | Process of esterification |
WO1985003084A1 (en) * | 1984-01-07 | 1985-07-18 | Henkel Kommanditgesellschaft Auf Aktien | Utilization of salicylic acid esters as perfuming substances, perfuming compositions containing them and new salicylic acid esters |
EP0280471A1 (de) * | 1987-02-23 | 1988-08-31 | BP Chemicals Limited | Verfahren zur kontinuierlichen Herstellung von Acetaten |
EP0304757A1 (de) * | 1987-08-25 | 1989-03-01 | BASF Aktiengesellschaft | Verfahren zur Herstellung von Carbonsäureestern |
WO1991019559A1 (de) * | 1990-06-15 | 1991-12-26 | Henkel Kommanditgesellschaft Auf Aktien | Verfahren zum durchführen einer gleichgewichtsreaktion unter anwendung von dämpfepermeation |
Also Published As
Publication number | Publication date |
---|---|
JPH09502735A (ja) | 1997-03-18 |
DE4344358A1 (de) | 1995-06-29 |
EP0735911A1 (de) | 1996-10-09 |
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