Classifications

• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
  • C12P7/00—Preparation of oxygen-containing organic compounds
  • C12P7/62—Carboxylic acid esters
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
  • C12P1/00—Preparation of compounds or compositions, not provided for in groups C12P3/00 - C12P39/00, by using microorganisms or enzymes

Definitions

• the present invention relates to a method for remov- ing water in enzyme-catalysed reactions, as well as an arrangement for implementing the method.
• Hydrolytic enzymes normally catalyse the hydrolysis of naturally occurring substances. By perform ⁇ ing such enzyme-catalysed reactions in an organic solvent of very low water content, one may reverse these pro ⁇ Des, that is, they may instead be used for synthesising products.
• Water is a reaction product in many synthetic reac ⁇ tions that are catalysed by hydrolases in organic solvents of low water content.
• EP Patent Applica ⁇ tion 0 257 388 discloses a transesterification reaction, whose yield is improved by generating a negative pressure in the gaseous phase above the reaction mixture or by bubbling nitrogen gas through the reaction mixture, thereby to remove water.
• the EP specification is clearly restricted to transesterification reactions, the desired reaction being not an ester synthesis but rather the replacement of fatty acids in existing esters, such as triglycerides.
• EP Patent Application 0064855 discloses the addi ⁇ tion of a drying agent to a reaction mixture, thereby to lower, the water activity in the mixture. If this process takes place in a closed vessel, the gaseous phase above the reaction mixture may, in addition, be contacted with the drying agent, so that water vapour can be directly adsorbed from the gaseous phase. Also, the ' drying agent may be replaced with a cold surface which enables the condensation of water vapour to water or ice. Such con ⁇ densation is preferably carried out under a reduced pres ⁇ sure.
• This publication is clearly restricted to the removal of water either as gas in the gaseous phase above the reaction mixture or by adsorption to the drying agent when directly contacted with the reaction mixture.
• EP Patent Application 0274798 water is removed by the addition of a molecular sieve directly the reaction mixture, by the provision of a cold surface in the gaseous phase, or by distillation at a temperature that is suffi ⁇ ciently low for the enzyme to remain active.
• EP Patent Application 0 383 405 discloses azeotropic distillation of a reaction mixture for removing the water formed.
• the idea is to use an alcohol in azeo ⁇ tropic distillation for removing water from the reaction mixture to a separate vessel in order to remove the pro ⁇ duct water from the azeotropic mixture by separate pro ⁇ Deads.
• the alcohol lost during distillation is replaced with fresh alcohol from a separate vessel ["Preferably, the azeotropic distillation of (III) (2-8 monoalcohol) and (III) added, are at the same rate"].
• the fact that the alcohol is added to the reaction mixture indicates that this is no integrated process.
• the alcohol removed is pre ⁇ ferably recycled to the reaction mixture after some or all of the water has been removed in a separate step.
• a suit- able distillation temperature is obtained by adjusting the pressure during distillation. No particular kind of sol ⁇ vent is used.
• the present invention provides a method for removing water in enzyme-catalysed reactions.
• the reaction is per- formed under reflux conditions in an organic solvent in the presence of an enzyme, an evaporated mixture of sol ⁇ vent, volatile reactants and water formed in the reaction being condensed.
• the condensed mixture is passed through a bed of water-adsorbing material where the water condensed with the solvent is adsorbed, and the solvent thus freed from water is recycled to the reaction mixture.
• the invention also provides an arrangement for imple ⁇ menting the method.
• This arrangement comprises a reaction vessel 1, a vapour pipe 2 for conveying an evaporated mix- ture of solvent, volatile reactants and water from the reaction vessel 1, a condenser 3 for condensing the evapo ⁇ rated mixture, a bed 4 of water-adsorbing material for adsorbing water from the condensed mixture, and a liquid pipe 5 for recycling the condensed solvent to the reaction vessel.
• the method according to the invention makes it pos ⁇ sible to considerably increase the rate of enzymatic syn ⁇ thesis reactions by performing the process in a refluxed solvent, the condensed mixture of solvent and water being, before recycling to the reaction mixture, conducted through a bed of water-adsorbing material incorporated in the reflux unit.
• water is continuously removed from the condensed solvent vapours, resulting in a constant flow of solvent which is recycled to the reaction mixture in the same way as in standard refluxing. This results in rapid production in a high yield of a high-purity product.
• the invention may be used in ester synthesis and other reactions, including reactions in which water is generated as well as reactions where it is important for or advantageous to the reaction process that water is removed.
• esters in which case a yield of more than 99% can be obtained within a few hours.
• the reaction conditions can be maintained so gentle that polyunsaturated esters can be produced without any peroxidation.
• an ester synthesis according to a preferred embo ⁇ diment of the invention use is conveniently made of a saturated or unsaturated monocarboxylic acid having 2-34 carbon atoms.
• Such acids are easily obtained from natural raw materials.
• Stearic acid, oleic acid and such polyunsa ⁇ turated fatty acids as arachidonic acid and a- and y-lino- lenic acid are particularly suitable.
• the starting alcohol is a monovalent alcohol having 1-24 carbon, atoms, preferably a primary alcohol, and is added in a ratio of 1-6 mole of alcohol to 1 mole of acid, preferably in a ratio of 1.25, at the beginning of the reaction. If need be, this ratio is maintained by periodic additions of dry alcohol to the reaction mixture. Conve ⁇ niently, ethanol and oleyl alcohol are used in these pro ⁇ Waits. Use may also be made of polyhydric alcohols, such as glycols and glycerol. Enzymes to be used in the process may be obtained from various sources, such as upases from the species Mucor, Rhizopus, Aspergillus, Humicola, Candida and Pseudomonas.
• the enzyme can be used in powder form, but is prefer- ably immobilised on a carrier to enable separation and re ⁇ use.
• Different immobilising methods can be employed, e.g. adsorption to the carrier, enclosure in gels, covalent bonding to the carrier, and deposit of the enzyme on the carrier.
• Suitable carriers are "Celit” (trademark, solu- tion of dicalcium silicate in dicalcium aluminate) or ion exchangers.
• a certain amount of water has to be present, asso ⁇ ciated with the enzyme.
• the optimum amount is sufficient for activating the enzyme without inducing the hydrolysis of the ester formed.
• the amount of water is below 15%, but above 0.1%, of the weight of the enzyme preparation.
• the water content of the enzyme is adjusted by the choice of carrier.
• a suitable carrier has such properties that it is able to retain enough water to keep the enzyme active, thus preventing deactivation.
• the water content of the solvent is adjusted by the choice of solvent.
• Solvents of highly non-polar nature (defined by a high "log P" value) only solve a minor amount of water, and are thus preferred.
• Polar solvents are often able to solve large amounts of water and may thus deactivate enzymes by removing water essential to the catalytic activity.
• the reaction temperature mainly depends on the boil- ing point of the solvent, and can thus be determined by the choice of a suitable solvent.
• the amount of solvent should be so high that the temperature under reflux con- ditions comes close to the boiling point of the solvent.
• the proportion of solvent is 20-98% v/w of the reaction mixture.
• the boiling point of the sol ⁇ vent lies within the range of 20-90°C.
• Suitable solvents are aliphatic hydrocarbons, and pentane is especially suitable for this type of reaction.
• the water-adsorbing material is a mole cular sieve, silica gel or natural products, such as starch and flour, e.g. maize starch and maize flour. It may be necessary to pretreat natural products by e.g. degreasing to avoid contamination of the reaction mixture. It may also be necessary to pretreat the adsorbing agent in alcohol to prevent alcohol from being adsorbed under refluxing. If such pretreatment occurs, the excess alcoho should be removed from the adsorbing agent before the reaction is initiated, so that it is possible to maintain a constant ratio between the reactants.
• Ester synthesis can be carried out batchwise or con ⁇ tinuously.
• the enzyme is recovered from the reaction mix- ture without being purified in any other way than by removing the excess solvent and the remaining alcohol by distillation.
• reaction time for batchwise processes is short, about 0.5-1.5 h, but may be longer in certain reac- tions.
• Fig. 1 is a schematic view of an embodiment of the inventive arrangement suited for use in small-scale processes
• Fig. 2 is a schematic view of another embodiment of the inventive arrangement suited for use in large-scale processes ⁇
• the method will be generally described with respect to the synthesis of esters and with reference to the draw ⁇ ings, where like reference numbers refer to like compo ⁇ nents.
• An evaporated solvent containing water formed in the reaction as well as volatile alcohol leaves the reaction vessel 1 and is conveyed up through the vapour pipe 2 in the form of vapour.
• the solvent vapours come into contact with the condenser 3, they are condensed to liquid, and the liquid is conducted through a bed 4 of water-adsorbing material. From the bed 4, the condensed solvent thus freed from water is recycled to the reaction vessel 1 via a liquid pipe 5 and the vapour pipe 2.
• the solvent may also be recycled via a separate pipe (not shown) from the top of the bed 4 to the reaction vessel 1.
• Large-scale reactions (about 500-2000 g), in which larger amounts of water are formed, are suitably carried out by means of the embodiment of the inventive arrange ⁇ ment shown in Fig. 2.
• This arrangement differs from that in Fig. 1 mainly in that a phase-separation tube 6 and a trap 7 are provided between the condenser 3 and the bed 4 of water-adsorbing material. At its outlet 9, the trap 7 is equipped with a bottom valve 8 which can be set in three positions.
• the valve 8 is kept closed (position 1), and the solvent is thus recycled directly from the phase-separation tube 6 to the reaction vessel 1 via an additional liquid pipe 10.
• a water-rich phase will collect in the trap 7.
• the liquid in the trap 7 can be drained through the valve 8 (position 2).
• the yield of the reaction is high (about 90%)
• the flow of condensed solvent from the trap 7 is conducted via the valve 8 (position 3) through the bed 4 of water-adsorbing material.
• the solvent is recycled to the reaction vessel 1 via the liquid pipe 5. In this position, liquid is prevented from flowing through the pipe 10 by the difference in height between the out- lets of the liquid pipe 10 and the liquid pipe 5. All solvent will thus pass through the bed 4, where the water entrained is adsorbed, before returning to the reaction vessel.
• Example 1 Example 1
• An activated molecular sieve (3 A, 8-12 mesh) was packed in a column for refluxing and pretreated with 100% ethanol for 15 min. The ethanol was decanted, and the molecular sieve was cleaned with 50 ml of dry hexane. A reaction vessel containing hexane and a few boiling stones was connected to the bottom of the reflux con ⁇ denser, and the molecular sieve was cleaned by refluxing hexane over the sieve for 15 min. The hexane that had undergone this process was tested for its content of ethanol by being poured into a measuring cylinder con ⁇ taining a known amount of water. The molecular sieve was regarded as sufficiently clean if no increase in volume took place in the aqueous phase.
• Example 3 It is possible to use other solvents as reaction media in the production of esters. Thus, the procedure of Example 1 was repeated but with oleic acid instead of stearic acid and with pentane instead of hexane. Ethyl oleate was formed in a yield of more than 99% within 120 min.
• Example 3
• Example 4 It is also possible to use other alcohols as starting material in the production of esters. Thus, the procedure of Example 1 was repeated, but the molecular sieve was not pretreated with alcohol. When 3-pentene-l-ol was esteri- fied with a stoichiometric amount of stearic acid, a degree of transformation of 97.2% was attained within 4 h.
• Example 4
• the reaction conditions of the invention are gentle and can be used for unsaturated and polyunsaturated acids without any formation of peroxide.
• oleic acid, lino- leic acid, ⁇ -linolenic acid, 2f-linolenic acid and arachi- donic acid were esterified with ethanol, as in Example 2.
• the reaction times were short, but per- oxidation was minimal also in the synthesis of ethyl-#- linolenate, which was much slower than the other ester syntheses.
• the peroxidation products were determined by standard methods, and the results are indicated in Table 2 below.
• the inventive method is suitably used for producing non-volatile esters, such as waxes.
• Oleyl alcohol was esterified with oleic acid in pen- tane as described in Example 1, apart from the fact that the molecular sieve was not pretreated with ethanol. Oleyloleate was obtained in a yield of 99.8% within 20 min, and there was no formation of peroxide (Table 3).

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Citations (3)

• 1991
  • 1991-12-19 SE SE9103767A patent/SE9103767L/sv not_active Application Discontinuation
• 1992
  • 1992-12-18 AU AU31760/93A patent/AU3176093A/en not_active Abandoned
  • 1992-12-18 WO PCT/SE1992/000877 patent/WO1993012241A1/en active Application Filing

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