WO2005056508A1 - Verfahren zur herstellung von tetrahydrogeranylaceton - Google Patents
Verfahren zur herstellung von tetrahydrogeranylaceton Download PDFInfo
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- WO2005056508A1 WO2005056508A1 PCT/EP2004/014070 EP2004014070W WO2005056508A1 WO 2005056508 A1 WO2005056508 A1 WO 2005056508A1 EP 2004014070 W EP2004014070 W EP 2004014070W WO 2005056508 A1 WO2005056508 A1 WO 2005056508A1
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- C07D473/26—Heterocyclic compounds containing purine ring systems with an oxygen, sulphur, or nitrogen atom directly attached in position 2 or 6, but not in both
- C07D473/32—Nitrogen atom
- C07D473/34—Nitrogen atom attached in position 6, e.g. adenine
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- C07C45/61—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups
- C07C45/62—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by hydrogenation of carbon-to-carbon double or triple bonds
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- C07C45/61—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups
- C07C45/67—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton
- C07C45/68—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
- C07C45/72—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction of compounds containing >C = O groups with the same or other compounds containing >C = O groups
- C07C45/74—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction of compounds containing >C = O groups with the same or other compounds containing >C = O groups combined with dehydration
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- C07D231/02—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings
- C07D231/10—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D231/12—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with only hydrogen atoms, hydrocarbon or substituted hydrocarbon radicals, directly attached to ring carbon atoms
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- C07D231/02—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings
- C07D231/10—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D231/14—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
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- C07D231/02—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings
- C07D231/10—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D231/14—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
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- C07D231/02—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings
- C07D231/10—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D231/14—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D231/18—One oxygen or sulfur atom
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- C07D231/00—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings
- C07D231/02—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings
- C07D231/10—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D231/14—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D231/38—Nitrogen atoms
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- C07D231/00—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings
- C07D231/54—Heterocyclic compounds containing 1,2-diazole or hydrogenated 1,2-diazole rings condensed with carbocyclic rings or ring systems
- C07D231/56—Benzopyrazoles; Hydrogenated benzopyrazoles
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- C07D—HETEROCYCLIC COMPOUNDS
- C07D233/00—Heterocyclic compounds containing 1,3-diazole or hydrogenated 1,3-diazole rings, not condensed with other rings
- C07D233/54—Heterocyclic compounds containing 1,3-diazole or hydrogenated 1,3-diazole rings, not condensed with other rings having two double bonds between ring members or between ring members and non-ring members
- C07D233/56—Heterocyclic compounds containing 1,3-diazole or hydrogenated 1,3-diazole rings, not condensed with other rings having two double bonds between ring members or between ring members and non-ring members with only hydrogen atoms or radicals containing only hydrogen and carbon atoms, attached to ring carbon atoms
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- C07D235/00—Heterocyclic compounds containing 1,3-diazole or hydrogenated 1,3-diazole rings, condensed with other rings
- C07D235/02—Heterocyclic compounds containing 1,3-diazole or hydrogenated 1,3-diazole rings, condensed with other rings condensed with carbocyclic rings or ring systems
- C07D235/04—Benzimidazoles; Hydrogenated benzimidazoles
- C07D235/06—Benzimidazoles; Hydrogenated benzimidazoles with only hydrogen atoms, hydrocarbon or substituted hydrocarbon radicals, directly attached in position 2
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- C07D—HETEROCYCLIC COMPOUNDS
- C07D249/00—Heterocyclic compounds containing five-membered rings having three nitrogen atoms as the only ring hetero atoms
- C07D249/02—Heterocyclic compounds containing five-membered rings having three nitrogen atoms as the only ring hetero atoms not condensed with other rings
- C07D249/08—1,2,4-Triazoles; Hydrogenated 1,2,4-triazoles
- C07D249/10—1,2,4-Triazoles; Hydrogenated 1,2,4-triazoles with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D249/12—Oxygen or sulfur atoms
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- C07D—HETEROCYCLIC COMPOUNDS
- C07D257/00—Heterocyclic compounds containing rings having four nitrogen atoms as the only ring hetero atoms
- C07D257/02—Heterocyclic compounds containing rings having four nitrogen atoms as the only ring hetero atoms not condensed with other rings
- C07D257/04—Five-membered rings
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- C07D401/00—Heterocyclic compounds containing two or more hetero rings, having nitrogen atoms as the only ring hetero atoms, at least one ring being a six-membered ring with only one nitrogen atom
- C07D401/02—Heterocyclic compounds containing two or more hetero rings, having nitrogen atoms as the only ring hetero atoms, at least one ring being a six-membered ring with only one nitrogen atom containing two hetero rings
- C07D401/12—Heterocyclic compounds containing two or more hetero rings, having nitrogen atoms as the only ring hetero atoms, at least one ring being a six-membered ring with only one nitrogen atom containing two hetero rings linked by a chain containing hetero atoms as chain links
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- C07D403/02—Heterocyclic compounds containing two or more hetero rings, having nitrogen atoms as the only ring hetero atoms, not provided for by group C07D401/00 containing two hetero rings
- C07D403/12—Heterocyclic compounds containing two or more hetero rings, having nitrogen atoms as the only ring hetero atoms, not provided for by group C07D401/00 containing two hetero rings linked by a chain containing hetero atoms as chain links
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- C07D409/00—Heterocyclic compounds containing two or more hetero rings, at least one ring having sulfur atoms as the only ring hetero atoms
- C07D409/02—Heterocyclic compounds containing two or more hetero rings, at least one ring having sulfur atoms as the only ring hetero atoms containing two hetero rings
- C07D409/04—Heterocyclic compounds containing two or more hetero rings, at least one ring having sulfur atoms as the only ring hetero atoms containing two hetero rings directly linked by a ring-member-to-ring-member bond
Definitions
- the present invention relates to a process for the preparation of tetrahydrogeranylacetone (hexahydropseudojonone) by aldol condensation of citral with acetone and subsequent hydrogenation.
- the invention further relates to the use of tetrahydrogeranylacetone obtained in this way for the production of phytol, isophytol, tocopherol and / or tocopherol derivatives.
- the invention relates to processes for the production of tocopherols and / or tocopherol derivatives.
- Tetrahydrogeranylacetone (THGAC, hexahydropseudojonone) is used as a starting material for the production of isophytol, which in turn is used as a starting material for the production of vitamin E and vitamin K (see, for example, Ullmann's Encyclopedia of Industrial Chemistry, 5th ed. On CD-Rom, "Vitamins” , chapter 4.11).
- PL-A 147748 describes a process for the production of ion by condensation of citral and acetone on basic ion exchangers at 56 ° C. Thereafter, acetone and citral are stirred discontinuously in a flask with the catalyst for 5 hours.
- the disadvantage of this process is the very low space-time yields.
- DE-A 33 19430 describes the preparation of higher ketones by condensation of methyl ketones and unsaturated aldehydes over mixed metal catalysts in the presence of hydrogen at 100 to 280 ° C. and 10 to 60 bar in a tubular reactor.
- a process for the production of pseudo-ionones by reacting citral with acetone using LiOH as a catalyst is described in US 4,874,900. Thereafter, the reaction is carried out batchwise or continuously at temperatures from -20 to 240 ° C. The pressure is adjusted so that the reaction mixture remains in the liquid phase at the appropriate temperature. In the case of discontinuous operation, the reactants are stirred in a vessel and the catalyst is filtered off after the reaction has ended, while in the continuous mode of operation the premixed reactants are pumped through a column filled with catalyst. In both cases, the reaction mixture becomes with after the end of the reaction CO 2 neutralized and the excess ketone distilled off. In this process, with a molar ratio of acetone to citral of 20 mol / mol, yields of 89.5% citral are achieved, which is insufficient for a large-scale process.
- DE-A 31 14071 describes a process for the preparation of pseudonones by reacting an aldehyde with an excess of a ketone at elevated temperature.
- EP-A 1 103538 relates to a process for the preparation of ⁇ , ⁇ -unsaturated keto compounds by base-catalyzed aldol condensation of aldehydes and / or ketones with 1 to 15 carbon atoms.
- EP-A 62291 discloses the continuous production of pseudoionone by reacting citral with acetone with NaOH catalysis in a tubular reactor.
- No. 2,272,122 describes the suspension hydrogenation of pseudoionone to hexahydropseudoionone at temperatures of 50 to 100 ° C. and increased pressure on Pd / C with hydrogen.
- GB 788,301 describes a process for the preparation of THGAC in which geranylacetone or dihydrogeranylacetone is hydrogenated to THGAC in the last step.
- WO 94/12457 describes the preparation of hexahydropseudo-ionone by hydrogenating pseudo-ionone with 5% Pd / C.
- the object of the present invention was to develop an overall process which makes it possible to provide the intermediate hexahydropseudojonone (tetrahydrogeranylacetone) which is central to the synthesis of phytol, isophytol, tocopherol and / or tocopherol derivatives in a technically simple and economical manner.
- the object was achieved according to the invention by providing a process for the preparation of tetrahydrogeranylacetone, comprising I. an aldol condensation of citral with acetone in the presence of an aqueous alkali metal hydroxide solution containing at least one alkali metal hydroxide to form a pseudoionone-containing condensate and II. Hydrogenation of the condensate.
- THGAC tetrahydrogeranylacetone
- the procedure is such that a. Citral, an excess of acetone and aqueous alkali solution are mixed at a temperature in the range from 10 to 120 ° C. to form a homogeneous solution, b. then the homogeneous reaction mixture is liquid, avoiding backmixing at a temperature which is 10 to 120 ° C. above the boiling point of acetone, under a pressure which is 10 6 to 10 7 Pa above the corresponding vapor pressure, but at least the intrinsic pressure of the Corresponds to the reaction mixture, passed through a reactor which allows a residence time of 2 to 300 minutes, c. the reaction mixture is cooled with relaxation, d. excess acetone removed with steam in countercurrent from the reaction mixture, e. the crude product thus obtained is purified on a rectification column and then f. the pseudo-ionone thus obtained is hydrogenated to tetrahydrogeranylacetone.
- An aqueous alkali solution means an aqueous solution of potassium hydroxide, sodium hydroxide or lithium hydroxide, but preferably sodium hydroxide solution.
- concentration of the alkali metal hydroxide used is between 0.005 and 50% by weight, preferably between 1 and 15% by weight.
- aqueous alkali lye is added to the homogeneous mixture of the starting materials citral, acetone and water at 10 to 120 ° C., preferably at temperatures below 50 ° C., as to dissolve homogeneously after thorough mixing.
- Any water and alkali hydroxide that separate out are preferably separated off before the remaining homogeneous reaction mixture, avoiding backmixing, at a temperature which is 10 to 120 ° C.
- the acetone above the boiling point of the lowest-boiling component (here the acetone) and a pressure p of 10 6 to 10 7 Pa, where p is the vapor pressure of the reaction mixture at the reaction temperature, is passed through a reactor which allows a residence time of 2 to 300 minutes, preferably 5 to 30 minutes.
- the reaction mixture is preferably cooled by depressurization, it being possible for some of the excess acetone to be evaporated and recycled.
- the remaining acetone is then advantageously removed from the reaction mixture with steam in countercurrent, the steam preferably containing so much of an acid which can be vaporized under the given conditions, such as, for example, formic acid or acetic acid, that the catalyst base is neutralized and a pH of 4 to 9 sets.
- the pseudoionone-containing crude product can then be dried and purified via a rectification column, preferably via a dividing wall column, as disclosed, for example, in DE-A 3302525 or in EP-A 804951. It frees the crude product in particular from excess citral and undesirable secondary components such. B.4-hydroxy-4-methyl-2-pentanone and / or 4-methyl-3-penten-2-one.
- These secondary components can advantageously e.g. by the action of a base in the presence of water, e.g. be split back into acetone by aqueous sodium hydroxide solution, if appropriate at elevated temperature.
- the acetone obtained in this way can be reused if necessary, preferably as part of the process according to the invention.
- the reaction is preferably carried out with a 5 to 50-fold, particularly preferably with a 20 to 25-fold molar excess of acetone in order to achieve an optimal yield with regard to the citral used.
- the unreacted portion of acetone is preferably separated off after the reaction zone at a pressure of 10 v to 10 9 mPa abs and fed back to the fresh acetone for synthesis.
- the water content of the citral-acetone mixture is also of particular importance. It was found that this influences the amount of alkali metal hydroxide which can be homogeneously dissolved in the aldehyde-ketone mixture.
- the water content of the aldehyde-ketone mixture is preferably between 1 and 15% by weight. It was also surprisingly found that the amount of alkali metal hydroxide dissolved influences the rate of conversion, but also the proportion of undesirable by-products. Furthermore, the removal of excess alkali upstream of the reactor is advantageous. In contrast to the prior art, this means that fewer by-products are formed. The latter plays especially with sensitive unsaturated aldehydes such as Citral plays an important role and lowers the yield.
- the water is advantageously introduced into the process via the proportion of the ketone component (here in the form of aqueous acetone) which is generated, for example, by steam stripping the reaction mixture after the reactor. It is of economic importance that the excess acetone can be separated off with little technical and energy expenditure, since a complex drying process before recycling is unnecessary.
- an anhydrous mixture of citral and acetone can be used and the required water (about 1 to 15% by weight) can be mixed in by using a very dilute alkali hydroxide solution.
- a mixture of citral and acetone with a very high water content can be used if a concentrated alkali hydroxide solution is added. A lower mixing temperature is required to avoid the uncontrolled start of the reaction.
- the consumption of alkali hydroxide increases, since this only partially passes into the organic phase. It partially extracts water from the citral-acetone mixture and has to be separated and disposed of.
- the homogeneous reaction solution is preferably heated under autogenous pressure in a tube reactor, the reaction temperature for a given residence time preferably being set so that the conversion of citral is 60 to 98%, particularly preferably 85 to 95%, unreacted citral being separated off and in the implementation is returned.
- the tubular reactor is dimensioned such that the average residence time is preferably between 2 and 300 minutes, in particular between 5 and 30 minutes, if possible in such a way that there is no backmixing.
- backmixing is minimized in the tubular reactor. This can be achieved, for example, by a sufficiently large reactor diameter to avoid turbulence, or else by any kind of laminar flow internals. This is surprising and contradicts the prior art, where e.g. According to DE-A 31 14071 tubular reactors must be such that there is a sufficiently turbulent flow under the reaction conditions.
- the reaction mixture is preferably let down to atmospheric pressure, where it cools down by the evaporation of part of the excess acetone.
- the remaining acetone is advantageously driven off in a countercurrent column with steam, to which an equimolar amount of a volatile acid is added, the catalyst base being neutralized and diluted by the condensate.
- the preferred use of column packs ensures that no significant amounts of other products are obtained at the top of the column in addition to acetone and water, the return flow to the column advantageously being set such that the acetone can be drawn off with the desired amount of water.
- a stripping column is preferably chosen which is filled with commercially available, ordered packing elements and is preferably sprinkled with liquid in an amount of 10 to 90% of the separated acetone.
- the amount of acid is advantageously dimensioned such that the pH value of 4 to 9 which is most favorable for further workup is established at this point.
- the recycling is advantageously carried out in a dividing wall column as described in EP-A 804 951, where there are preferably 2 side draws in order to obtain both main fractions (pseudo-ionone and citral) in sufficient purity in one step.
- the hydrogenation of the pseudoionone thus obtained can in principle be carried out by any method which is suitable for carrying out the conversion of pseudoionone to tetrahydropseudoionone (THGAC).
- TGAC tetrahydropseudoionone
- the reagents to be used and the reaction parameters to be observed can be varied over a wide range.
- the hydrogenation is carried out in such a way that the pseudo-ionone obtained is suspended in the liquid phase, in which particles of a catalyst are used, for the preferential hydrogenation of carbon-carbon double bonds over carbon-oxygen double bonds is capable, in the presence of a hydrogen-containing gas, through a device which inhibits the transport of the catalyst particles.
- the device which inhibits the transport of the catalyst particles preferably has openings or channels whose hydraulic diameter is 2 to 2000 times, in particular 5 to 500 times, particularly preferably 5 to 100 times the average diameter of the catalyst particles.
- the hydraulic diameter is a parameter familiar to the person skilled in the art for describing the equivalent diameter of non-circular channel structures.
- the hydraulic diameter of an opening is defined as the quotient of 4 times the cross-section of the opening and its circumference.
- the hydraulic diameter can be as
- the openings or channels of suitable devices generally have a hydraulic diameter of 0.5 to 20 mm, preferably 1 to 10 mm, particularly preferably 1 to 3 mm.
- catalyst particles with an average diameter of 0.0001 to 2 mm, preferably 0.001 to 1 mm, particularly preferably 0.005 to 0.1 mm are used.
- the device which inhibits the transport of the catalyst particles can consist of a bed, a knitted fabric, an open-cell foam structure, preferably made of plastic, e.g. Polyurethane or melamine resin, or ceramic, or a packing element as is basically, i.e. its geometrical shape, already known from the distillation and extraction technology, exist.
- the packs basically have a hydraulic diameter which is substantially smaller, regularly by a factor of 2 to 10, than comparable internals in the area of distillation and extraction technology.
- Metal mesh packs or wire mesh packs are particularly suitable as packing elements, e.g. of the type Montz A3, Sulzer BX, DX and EX. Instead of metal mesh packs, packs made of other woven, knitted or felted materials can also be used. Packs of flat or corrugated sheets are also suitable, preferably without perforation or other larger openings, for example in accordance with the types Montz B1 or Sulzer Mellapak. Packings made of expanded metal, e.g. Montz BSH packs. What is decisive for the suitability of a package in the context of the present invention is not its geometry, but rather the opening sizes or channel widths in the package which arise for the current flow.
- the surfaces of the device facing the liquid phase have a roughness in the range from 0.1 to 10 times, preferably from 0.5 to 5 times, the average diameter of the catalyst particles.
- Materials are preferred whose surfaces have a mean roughness value R a (determined according to DIN 4768/1) of 0.001 to 0.01 mm.
- R a determined according to DIN 4768/1
- a corresponding surface roughness can be achieved when using wire mesh packings made of stainless steel by thermal treatment in the presence of oxygen, for example by tempering the mesh in air at a temperature of about 800 ° C.
- the liquid phase preferably contains at least 80% by weight, in particular at least 90% by weight, of hexahydro-pseudo-ionone, ie it preferably contains no large amounts of diluent.
- the liquid phase can contain diluents, such as CrC 4 alkanols, for example methanol.
- Hydrogen gas with a purity of at least 99.5% by volume is generally used as the hydrogen-containing gas. It is used in an at least stoichiometric amount, based on the carbonyl compound contained in the liquid phase, usually in an excess of 1 to 20%.
- a commercially available suspension catalyst which is capable of preferentially hydrogenating carbon-carbon double bonds over carbon-oxygen double bonds can be used as the catalyst.
- Particularly suitable catalysts are those which contain at least palladium as the active component.
- the catalyst can also contain other active components, such as zinc, cadium, platinum, silver or a rare earth metal such as cerium.
- the catalyst can be used in metallic and / or oxidic form.
- the active components are preferably applied to a carrier material. Suitable carrier materials are, for example, SiO 2 , TiO 2 , ZrO 2 , Al 2 O 3 or carbon such as graphite, carbon black or activated carbon. Activated carbon is preferred because of its easy suspendability.
- the palladium content is preferably 0.1 to 10% by weight, in particular 0.5 to 7% by weight and particularly preferably 2 to 6% by weight, based on the total weight of the catalyst.
- the suspended catalyst material can be introduced into the liquid phase and distributed therein using conventional techniques.
- the device which inhibits the transport of the catalyst particles is usually built into a reactor which is arranged in such a way that the reaction mixture is forced through the device as it passes through the reactor, i.e. the internals usually fill the entire free cross-section of the reactor.
- the internals preferably, but not necessarily, extend over the entire extent of the reactor in the direction of flow of the liquid phase.
- reactor shapes such as jet nozzle reactors, bubble columns or tube bundle reactors.
- a vertically arranged bubble column or a tube bundle reactor in which the internals are accommodated in the individual tubes are particularly suitable.
- the hydrogen-containing gas and the liquid phase are preferably passed through the reactor in cocurrent, preferably counter to the direction of gravity.
- the gas phase is intimately mixed with the liquid phase, for example by means of an injector nozzle.
- the empty tube velocity of the liquid phase is preferably more than 100 m 3 / m 2 h, in particular 100 to 250 m 3 / m 2 h, that of the gas phase more than 100 Nm 3 / m 2 h, in particular 100 to 250 Nm 3 / m 2 h , In order to achieve sufficiently high empty tube velocities, it is preferred to return partial streams of the gas and liquid phase that leave the reactor.
- the catalyst particles suspended in the hydrogenation discharge are separated off by customary methods, for example by sedimentation, centrifugation, cake filtration or crossflow filtration.
- the hydrogenation process is preferably carried out at a pressure of 1 to 100 bar, particularly preferably from 1 to 50 bar and in particular from 1 to 20 bar.
- the reaction temperature is preferably 20 to 150 ° C, particularly preferably 20 to 120 ° C and in particular 40 to 80 ° C.
- Figure 1 shows schematically a plant suitable for carrying out the preferred hydrogenation process with a reactor (bubble column) 1 with a packing 2 which inhibits the transport of the catalyst particles.
- Liquid is introduced into the reactor via lines 3 and hydrogen gas via line 4.
- the circulating gas 5 is mixed in with the mixing nozzle 6 with fresh gas and the suspension 11 circulated by the pump 14.
- the reactor discharge is fed via line 7 into the separating vessel 8, in which the gas phase is separated off and discharged via line 9.
- a partial stream of this gas quantity is withdrawn via line 10 and the remaining amount is fed via line 5 into the reactor.
- the suspended catalyst remains in the reactor system in that it is retained via a crossflow filter 12 and only catalyst-free liquid phase emerges via line 13 and is removed.
- the temperature in the reactor system can be set in a targeted manner via the heat exchanger 15.
- FIG. 2 shows schematically a layer of a folded fabric. Packs which can be used according to the invention are obtained if several of these layers are arranged one above the other. Each layer comprises channels with a cross section in the form of an isosceles triangle with the leg length s, the base b and the height h.
- Pseudoionons are obtained tetrahydrogeranylacetone, which is particularly suitable as a starting or intermediate stage for the production of phytol, isophytol, tocopherol and / or tocopherol derivatives.
- the present invention accordingly relates to the use of the tetrahydrogeranylacetone produced by the process according to the invention for the production of the valuable or active substances mentioned.
- the compounds mentioned are generally used widely as additives or active ingredients for cosmetic and pharmaceutical preparations or applications and also, inter alia, in human and animal nutrition.
- Another aspect of the invention relates to a particularly economical and technically advantageous overall process for the preparation of tocopherol and / or tocopherol derivatives, which comprises the following steps: a) the preparation of tetrahydrogeranylacetone according to the process described above, b) a reaction of the tetrahydrogeranylacetone thus obtained with a vinyl magnesium halide to give 3,7,11-trimethyl-1-dodecen-3-ol c) a reaction of the 3,7,11-trimethyl-1-dodecen-3-ol thus obtained with diketene or acetoacetic ester to give the corresponding ester d) a rearrangement of the ester thus obtained by Carroll reaction to 6,10,14, trimethyl-5-pentadecen-2-one, e) a reaction of 6,10,14, trimethyl-5-pentadecen-2-one thus obtained with Hydrogen to 6,10,14-trimethyl-pentadecan-2-one, f) a reaction of
- tocopherol and / or tocopherol derivatives can also advantageously be produced using the process according to the invention by using an overall process comprising the following steps: a) an aldol condensation of citral with acetone in the presence of a basic substance to form a condensate containing pseudoionone, b) a hydrogenation of the pseudoinone contained in the condensate to 6,10-dimethyl-2-undecanone, c) a reaction of 6,10-dimethyl-2-undecanone thus obtained with acetyl in the presence of a basic compound to form 3,7, 11-Trimethyl-1-dodecin-3-ol, d) a reaction of 3,7,11-trimethyl-1-dodecin-3-ol thus obtained with hydrogen in the presence of a catalyst containing palladium, silver and / or bismuth and carbon monoxide to 3,7,11-trimethyl-1-dodecen-3-ol, e) a reaction of 3,7,
- the acetone was completely expelled from the product mixture by the water vapor and concentrated in the rectifying section of the stripping column. This gave about 8,600 kg / h of acetone with a water content of about 5-6%, which was added after the addition of about 400 kg / h of dry acetone and fed back to the reactor.
- the pseudo-ionone obtained as the crude product was continuously drawn off together with the condensed water at the lower end of the stripping column at a temperature of> 95 ° C.
- the phases were separated and the condensation water from the aftertreatment tion (see Example 1b), the pseudo-ionone thus obtained was injected at 50 mbar into a flash container, where residues of low boilers and dissolved water were separated off, which were likewise fed to the aftertreatment.
- the liquid discharge from the flash container was continuously rectified in a dividing wall column with 2 side draws and separated into 4 fractions: further low boilers were removed overhead and were likewise fed to the aftertreatment. Approx. 80 kg / h of citral were separated off at the upper side discharge of the discharge side, which were returned to the process. Approx. 1100 kg / h pseudo-ionone were obtained on the lower side discharge of the discharge side.
- the column bottom was discharged continuously and fed to a downstream short path distillation, in which entrained product of value was separated off and returned to the
- HMP hydroxymethylpentanone
- MO mesityl oxide
- the water phase was made alkaline with sodium hydroxide solution, heated with steam and introduced into the side of a stripping column with an ordered packing.
- the stripping column was heated in countercurrent with steam.
- the condensation products were split into acetone, the acetone formed was stripped off together with about the same amount of water vapor overhead and fed to the acetone recovery (Exa)).
- the depletion based on HMP in the extraction water was> 90%.
- the reactor discharge was freed of excess hydrogen in a gas separator and the separated hydrogen was fed back into the reactor.
- the liquid phase was continuously pumped back into the reactor via crossflow filters. This gave 1030 kg / h of tetrahydrogeranylacetone, which can be fed to the tocopherol without further treatment of the subsequent process step in the manufacturing process.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Pyrane Compounds (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/596,335 US7411098B2 (en) | 2003-12-15 | 2004-12-10 | Method for the production of tetrahydrogeranylacetone |
JP2006543486A JP2007516250A (ja) | 2003-12-15 | 2004-12-10 | テトラヒドロゲラニルアセトンの製造方法 |
EP04801223A EP1697292A1 (de) | 2003-12-15 | 2004-12-10 | Verfahren zur herstellung von tetrahydrogeranylaceton |
CA002548262A CA2548262A1 (en) | 2003-12-15 | 2004-12-10 | Method for the production of tetrahydrogeranylacetone |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10359026A DE10359026A1 (de) | 2003-12-15 | 2003-12-15 | Verfahren zur Herstellung von Tetrahydrogeranylaceton |
DE10359026.9 | 2003-12-15 |
Publications (1)
Publication Number | Publication Date |
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WO2005056508A1 true WO2005056508A1 (de) | 2005-06-23 |
Family
ID=34672819
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2004/014070 WO2005056508A1 (de) | 2003-12-15 | 2004-12-10 | Verfahren zur herstellung von tetrahydrogeranylaceton |
Country Status (7)
Country | Link |
---|---|
US (1) | US7411098B2 (de) |
EP (1) | EP1697292A1 (de) |
JP (1) | JP2007516250A (de) |
CN (1) | CN1894190A (de) |
CA (1) | CA2548262A1 (de) |
DE (1) | DE10359026A1 (de) |
WO (1) | WO2005056508A1 (de) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2020099461A1 (en) | 2018-11-13 | 2020-05-22 | Basf Se | Apparatus for and process of making pseudoionone and hydroxy pseudoionone |
WO2020099452A1 (en) | 2018-11-13 | 2020-05-22 | Basf Se | Process of making pseudoionone and hydroxy pseudoionone in aqueous mixtures comprising citral and acetone, comprising adding first and second amounts of hydroxide |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
TW200842132A (en) * | 2007-04-20 | 2008-11-01 | Chi Mei Corp | Apparatus for hydrogenation and method for hydrogenating conjugated diene polymer by employing the apparatus |
CA2756362C (en) | 2010-12-22 | 2018-07-31 | Sulzer Chemtech Ag | Method of mass transfer, structured packing and mass transfer apparatus for a small liquid load |
CN109651118A (zh) * | 2018-12-25 | 2019-04-19 | 万华化学集团股份有限公司 | 一种植酮的制备方法 |
CN111825538B (zh) * | 2020-07-13 | 2022-08-05 | 万华化学集团股份有限公司 | 一种连续化生产假性紫罗兰酮的方法 |
CN115322084B (zh) * | 2022-07-28 | 2023-12-19 | 万华化学集团股份有限公司 | 一种假性紫罗兰酮生产过程提高丙酮利用率的方法 |
Citations (3)
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EP0062291A1 (de) * | 1981-04-08 | 1982-10-13 | BASF Aktiengesellschaft | Verbessertes Verfahren zur Herstellung mehrfach ungesättigter Ketone |
WO1994012457A1 (en) * | 1992-11-25 | 1994-06-09 | Loyola University Of Chicago | Process for preparing tertiary alkynols |
WO2002072522A1 (en) * | 2001-03-14 | 2002-09-19 | Degussa Ag | Improved process for the preparation of 6-methylheptanone |
Family Cites Families (8)
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US2272122A (en) * | 1940-10-05 | 1942-02-03 | Lee John | Process for producing hexahydropseudoionone |
GB788301A (en) | 1954-02-26 | 1957-12-23 | Hoffmann La Roche | A process for the manufacture of 6, 10-dimethyl-undecanone-(2) |
US3480577A (en) * | 1965-12-27 | 1969-11-25 | Shell Oil Co | Paint compositions comprising epoxy resin ester,pigment and glass fibers or polypropylene powder |
DE3319430A1 (de) | 1983-05-28 | 1984-11-29 | Basf Ag, 6700 Ludwigshafen | Verfahren zur herstellung von ketonen |
PL147748B1 (en) | 1986-10-12 | 1989-07-31 | Procedure for the receiving of ionones and methyl ionones | |
US4874900A (en) * | 1987-06-16 | 1989-10-17 | Union Camp Corporation | Preparation of pseudoionones |
DE19814879A1 (de) * | 1998-04-02 | 1999-10-07 | Basf Ag | Verfahren zur selektiven Flüssigphasenhydrierung von alpha,beta-ungesättigten Carbonylverbindungen |
DE19956410A1 (de) | 1999-11-24 | 2001-05-31 | Oxeno Olefinchemie Gmbh | Verfahren zur Durchführung von Aldolkondensationen |
-
2003
- 2003-12-15 DE DE10359026A patent/DE10359026A1/de not_active Withdrawn
-
2004
- 2004-12-10 CN CNA2004800374358A patent/CN1894190A/zh active Pending
- 2004-12-10 US US10/596,335 patent/US7411098B2/en not_active Expired - Fee Related
- 2004-12-10 EP EP04801223A patent/EP1697292A1/de active Pending
- 2004-12-10 JP JP2006543486A patent/JP2007516250A/ja not_active Withdrawn
- 2004-12-10 WO PCT/EP2004/014070 patent/WO2005056508A1/de not_active Application Discontinuation
- 2004-12-10 CA CA002548262A patent/CA2548262A1/en not_active Abandoned
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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EP0062291A1 (de) * | 1981-04-08 | 1982-10-13 | BASF Aktiengesellschaft | Verbessertes Verfahren zur Herstellung mehrfach ungesättigter Ketone |
WO1994012457A1 (en) * | 1992-11-25 | 1994-06-09 | Loyola University Of Chicago | Process for preparing tertiary alkynols |
WO2002072522A1 (en) * | 2001-03-14 | 2002-09-19 | Degussa Ag | Improved process for the preparation of 6-methylheptanone |
Non-Patent Citations (1)
Title |
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K. U. BALDENIUS ET AL.: "Ullmann's Encyclopedia of Industrial Chemistry - Vitamins - 4. Vitamin E", 15 June 2000, WILEY VCH, XP002321031 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2020099461A1 (en) | 2018-11-13 | 2020-05-22 | Basf Se | Apparatus for and process of making pseudoionone and hydroxy pseudoionone |
WO2020099452A1 (en) | 2018-11-13 | 2020-05-22 | Basf Se | Process of making pseudoionone and hydroxy pseudoionone in aqueous mixtures comprising citral and acetone, comprising adding first and second amounts of hydroxide |
Also Published As
Publication number | Publication date |
---|---|
EP1697292A1 (de) | 2006-09-06 |
US7411098B2 (en) | 2008-08-12 |
JP2007516250A (ja) | 2007-06-21 |
CN1894190A (zh) | 2007-01-10 |
US20070167655A1 (en) | 2007-07-19 |
DE10359026A1 (de) | 2005-07-21 |
CA2548262A1 (en) | 2005-06-23 |
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