FR3001215A1 - Purifying flow obtained from production process of natural vanillin used as flavoring agent in foodstuffs, by distilling the flow for the separation of natural vanillin and vanillin alcohol, and recovering a distilled natural vanillin flow - Google Patents

Abstract

The present invention relates to a process for purifying a stream (F1) derived from a process for producing natural vanillin, said stream (F1) comprising natural vanillin and at least vanillic alcohol, said process comprising the distillation said flow (F1) allowing the separation of the natural vanillin from the vanillic alcohol, and the recovery of a distilled vanillin stream.

Description

The present invention relates to the purification of natural vanillin by distillation, in particular by batch distillation or by continuous distillation.

Vanillin can be obtained by two distinct routes: a so-called natural pathway based on a biotechnological process comprising in particular the cultivation of a microorganism (fungi, bacteria, etc.) capable of allowing the biotransformation of a vanillin fermentation substrate. It is particularly known from EP0885968 and EP0761817 such a process in which the fermentation substrate is ferulic acid. This process results in the preparation of a vanillin called natural vanillin; a so-called synthetic route comprising conventional chemical reactions from guaiacol that does not involve a microorganism. This process results in the preparation of a vanillin called synthetic vanillin. Currently, natural vanillin, obtained by the so-called natural route, is purified by extraction with a solvent followed by crystallization. This process leads to a vanillin in specification limit: medium purity, colored, and a yield of the order of 90%.

The crystallization step has the disadvantage of requiring the use of organic solvents. The use of such solvents, although allowed, may have toxicological and / or environmental disadvantages. Now, currently, no one is able to provide a process for purifying natural vanillin that does not require the use of organic crystallization solvent. Methods for purifying synthetic vanillin by distillation are known. However, the flows at the end of the process for preparing vanillin by natural route or by synthetic route are quite distinct. The output flow of the natural vanillin preparation process typically comprises natural vanillin, vanillyl alcohol and a solvent, preferably a food solvent, for example ethyl acetate. This stream may also comprise vanillic acid, ferulic acid, guaiacol, benzoic acid, dimers and trimers, guaiacol derivatives and water. The output flow of synthetic vanillin preparation process typically comprises synthetic vanillin, ortho-vanillin, trimers, guaiacol and DFG (Diformaldehyde gaiacol). The way of apprehending these different flows is therefore distinct.

An object of the present invention is therefore to provide a process for purifying natural vanillin, in particular that does not require the use of a solvent.

Another object of the present invention is to provide a process for purifying natural vanillin that is simple to implement and can be implemented continuously to be compatible with industrial processes. In particular, the present invention seeks the provision of a natural vanillin purification process leading to a yield greater than 90%, preferably greater than 95%. Yet another object of the present invention is to provide a method for purifying natural vanillin that can be used to obtain, according to the desired specifications: a very pure natural vanillin, for example with a purity greater than or equal to 99%; or a natural vanillin of less purity, for example of purity of 96 to 98.9% and possessing, due to the presence of certain impurities, organoleptic properties different from those of the very pure natural vanillin and which are close to the organoleptic properties vanilla pod. The process according to the invention therefore advantageously makes it possible to control the level of residual impurities and in particular those having a positive influence on the organoleptic quality of the final natural vanillin. Natural vanillin being a thermosensitive product (especially formation of trimers by heating vanillin), another objective of the present invention is to provide a purification process that retains all the properties of vanillin.

Still other objects will appear on reading the description of the invention which follows. The natural vanillin according to the invention, obtained by the process of the invention, is a natural flavoring substance according to Article 9.2 (c) of Regulation EC1334 / 2008. That is to say a flavoring substance obtained by physical, enzymatic or microbiological processes from materials of plant, animal or microbiological origin taken as such or after processing for human consumption by one or more of the processes traditional food preparation. A natural flavoring substance is a naturally occurring and naturally occurring substance. The present invention relates to a process for purifying a stream from a process for producing natural vanillin, said stream comprising vanillin. natural and at least vanillic alcohol, by distillation allowing the separation of natural vanillin from vanillic alcohol.

In the context of the present invention, the term "process for the production of natural vanillin" means processes for the preparation of vanillin by biotechnological means. Such methods include in particular the cultivation of a microorganism capable of allowing the biotransformation of a vanillin fermentation substrate. It is particularly known from EP0885968 and EP0761817 such a method wherein the fermentation substrate is ferulic acid. In the context of the present invention, the term "natural vanillin" vanillin obtained by preparation processes as defined above.

In the context of the present invention, the term "ultra-light impurities" or "ultra-light" compounds whose volatility is higher than that of natural vanillin under the conditions of pressure and temperature considered. The ratio of the ultra-light vapor pressure to the vapor pressure of the vanillin is from 60 to 200 to 134 ° C (or the distillation temperature). Among the ultra-light impurities include ethyl acetate. The term "light impurities" or "light" means compounds whose relative volatility is intermediate between that of ultra-light and that of natural vanillin under the conditions of pressure and temperature considered. Among the light impurities may be mentioned benzoic acid and guaiacol. "Heavy impurities" or "heavy" are compounds whose relative volatility is lower than that of natural vanillin under the pressure and temperature conditions considered. The ratio of the vapor pressure of the heavy metals to the vapor pressure of the vanillin is between 0.3 and 0.7 at 150 ° C. (or at the distillation temperature). Among the heavy impurities mention may be made of dimers, trimers of vanillin (that is to say compounds having a backbone having two respectively three phenyl groups, the dimers being advantageously chosen from diphenylmethanes), vanillic alcohol, vanillic acid, ferulic acid, benzoates, especially sodium benzoate, guaiacol derivatives, for example 4-methyl guaiacol and 4-ethyl guaiacol. In general, volatility is the ability of a substance to vaporize.

At the end of the process for preparing natural vanillin, a liquid stream (F1) is obtained that includes natural vanillin, ultra-light, light and heavy ones. In a particular embodiment, the ultralights represent from 50 to 90% by weight of the flux (F1), the light ones represent from 0.1 to 10% by weight of the flux (F1), the heavy ones represent from 0.1 to 15% by weight of the flow (F1), the natural vanillin represents from 5 to 35% by weight of the flow (F1). Preferably, the ultra-light represent from 60 to 80% by weight of the flux (F1), the light ones represent from 0.5 to 5% by weight of the flux (F1), the heavy ones represent from 1 to 10% by weight of the flow (F1), natural vanillin represents from 10 to 30% by weight of the flow (F1).

The composition of the flow (F1) of departure is given as an indication and the method of the invention is also suitable for mixtures comprising more or less natural vanillin.

In a particular embodiment, the flow (F1) comprises: from 5 to 35% by weight of natural vanillin, in particular from 10 to 30% by weight; from 0.05 to 10% by weight of vanillic alcohol, in particular from 0.1 to 5% by weight; from 0.0 to 2% by weight of vanillic acid, especially from 0.01 to 0.6% by weight; from 0.0 to 2% by weight of ferulic acid, especially from 0.01 to 0.9% by weight; from 0.0 to 2% by weight of guaiacol, in particular from 0.01 to 0.6% by weight; from 0.0 to 5% by weight of dimers and trimers, preferably from 0.05 to 5% by weight of dimers and trimers, in particular from 0.1 to 5% by weight; the dimers and trimers being compounds having a backbone respectively having two or three phenyl groups, the dimers being advantageously chosen from diphenylmethanes; from 0.0 to 5% by weight of various organic compounds which are also biosynthesized (for example 4-methyl guaiacol, 4-ethyl guaiacol and / or 4-vinyl guaiacol), preferably from 0.01 to 5% by weight, in particular from 0.05 to 1% by weight; from 0.0 to 10% by weight of benzoic acid, preferably from 0.01 to 10% by weight of benzoic acid, in particular from 0.05 to 5% by weight; from 0.0 to 5% by weight of water, preferably from 0.01 to 5% by weight of water, especially from 0.05 to 3% by weight; the addition to 100% by weight being a food solvent, for example ethyl acetate. Preferably, the operating pressure during the distillation is between 2 and 10 mbar, preferably between 3 and 6 mbar, for example it is 4 mbar. In the context of the present invention, the term "service pressure" means the pressure at the top of the distillation column. Advantageously, the pressure drop in the distillation column must be as low as possible. Preferably, the pressure drop is between 1 and 10 mbar, preferably between 2 and 8 mbar, for example the pressure drop is 3 or 4 mbar.

In the context of the present invention, and unless otherwise indicated, the expression "between x and y" includes the values x and y. In the context of the invention this expression also means "from x to y".

In the process according to the invention, one or more distillation columns are used. Preferably, the distillation column or columns comprise from 7 to 40 theoretical plates, preferably from 12 to 30 theoretical plates.

Advantageously, the process according to the invention makes it possible to obtain a natural vanillin of purity greater than or equal to 96%, preferably greater than or equal to 98%. In one embodiment, the process according to the invention makes it possible to obtain a very pure natural vanillin, especially with a purity greater than or equal to 99% and preferably containing less than 1000 ppm of vanillic alcohol. This embodiment can be obtained by adapting the distillation parameters. In another embodiment, the process according to the invention makes it possible to obtain a natural vanillin of lesser purity, for example of purity of 96 to 98.9%, and comprising impurities conferring on the flow of natural vanillin obtained different organoleptic properties. that of natural vanillin very pure and close to those of the vanilla pod. In this embodiment, the final flow of natural vanillin may comprise up to 3% by weight of impurities. Most of the impurities include vanillic alcohol, and dimers and / or trimers, in particular diphenylmethanes, which can represent up to 1% by weight of the flux, and in the minority vanillic acid, guaiacol, benzoic acid and biosynthesized organic compounds, each of which may be present up to 500 ppm in the stream. This embodiment can be obtained by adapting the distillation parameters. In the context of the process of the invention, a vanillin trimerization chemical reaction can occur which affects the yield of vanillin. The process for purifying natural vanillin by distillation according to the present invention can be carried out in different ways: by discontinuous distillation; - by continuous distillation; or - by continuous distillation on a Divided Wall Column (DWC). Discontinuous Distillation In one embodiment, the process according to the invention is carried out by discontinuous distillation. The process then comprises different unitary distillation operations allowing distinct separation of ultra-light, light, vanillin and heavy.

In the batch process, the stream (F1) is fed into a distillation column. The method makes it possible to recover: in a first fraction, the ultra-light ones; in a second fraction, the light ones may possibly comprise natural vanillin at a low concentration; in a third fraction, the stream comprising natural vanillin; and in the distillation pellet the heavy ones which may optionally comprise natural vanillin at a low concentration. In this embodiment, the term "low concentration" means a concentration of preferably at most 10%, preferably at most 5%, for example at most 3% by weight relative to the total weight of the fraction. The first, second and third fractions can advantageously be recovered by condensation using conventional devices known to those skilled in the art.

Those skilled in the art are perfectly able to set the distillation parameters such as, in particular, the diameter of the column, the column height and the packing. We will simply recall the following. The size (especially the diameter) of the distillation columns depends on the circulating flow and the internal pressure. Their sizing will therefore be mainly according to the mixing rate to be treated. It will be specified that the column may be lined with either trays or ordered or woven packing, as is well known to those skilled in the art. The installation being determined, the person skilled in the art adjusts the operating parameters of the column.

Preferably, the distillation column comprises from 7 to 30 theoretical plates, preferably from 5 to 15 theoretical plates, for example 7 to 10 theoretical plates. Preferably, the packing of the column is a surface woven lining of 400 to 600 m 2 / m 3.

This distillation process makes it possible to obtain natural vanillin with a yield of 90% to 95%, preferably of 90% to 93%. In one embodiment, the process according to the invention makes it possible to obtain a very pure natural vanillin, especially with a purity greater than or equal to 99% and preferably containing less than 1000 ppm of vanillic alcohol. In another embodiment, the process according to the invention makes it possible to obtain a natural vanillin of lesser purity, for example of purity of 96 to 98.9%, and comprising impurities conferring on the flow of natural vanillin obtained different organoleptic properties. that of natural vanillin very pure and close to those of the vanilla pod. In this embodiment, the final flow of natural vanillin may comprise up to 3% by weight of impurities. Most of the impurities include vanillic alcohol, and dimers and / or trimers, in particular diphenylmethanes, which can represent up to 1% by weight of the flux, and in the minority vanillic acid, guaiacol, benzoic acid and biosynthesized organic compounds, each of which can be present up to 500 ppm in the stream. Continuous distillation In one embodiment, the process according to the invention is carried out by continuous distillation. In a particular embodiment, the process carried out by continuous distillation comprises the following steps: a) in a first step, the flow (F1) is treated in order to eliminate the ultra-light (flux (F11)) that it contains and more particularly ethyl acetate, the flow thus obtained comprising natural vanillin, light and heavy is called flux (F2); b) in a second step, the flow (F2) is fed into a first distillation column, for recovering at the top of distillation a flow (F12) comprising light and possibly comprising a low concentration of natural vanillin and in the foot of distillation a stream (F13) comprising natural vanillin and heavy and possibly comprising a low concentration of light; c) the flow (F13) is supplied continuously in a second distillation column for recovering at the distillation head a stream (F14) comprising natural vanillin and at the bottom of a distillation stream (F15) comprising the heavy and optionally a low concentration of natural vanillin. Those skilled in the art are perfectly able to set the distillation parameters such as, in particular, the diameter of the column, the column height and the packing. We will simply recall the following. The size (especially the diameter) of the distillation columns depends on the circulating flow and the internal pressure. Their sizing will therefore be mainly according to the mixing rate to be treated. It will be specified that the column may be lined with either trays or ordered or woven packing, as is well known to those skilled in the art. The installation being determined, the person skilled in the art adjusts the operating parameters of the column. In this embodiment, the term "low concentration" is understood to mean a concentration of preferably not more than 5%, preferably not more than 3%, for example not more than 2% by weight relative to the total weight of the According to a preferred embodiment of the topping / tailing scheme, at least a portion of the stream (F15) is mixed with the stream (F14) so as to be able to vary the final composition of a purified natural vanillin stream.

Preferably, the flow (F12) at the top of distillation in step b) comprises the light ones, and in particular benzoic acid, guaiacol and possibly a low concentration of natural vanillin. Preferably, the distillation column of step b) comprises from 20 to 35 theoretical plates, preferably from 23 to 30 theoretical plates. The distillation column of step b) comprises in particular from 8 to 15 theoretical plates for the concentration section and from 12 to 20 theoretical plates for the depletion section, preferably from 10 to 13 theoretical plates for the concentration section. and from 13 to 17 theoretical plateaus for the exhaustion section.

The distillation column of step b) can be a distillation column equipped with an ordered packing on a height of 2x2600 mm to 2x3000 mm (2600mm to 3000 mm for each of the concentration and exhaustion sections). The lining of the column is preferably a woven lining due to the very low operating pressures.

In the column of step b), the operating pressure is preferably between 2 and 10 mbar, preferably between 3 and 6 mbar. The pressure drop is preferably 1 to 10 mbar, preferably 1 to 8 mbar. In step b), the reflux ratio is between 10 and 30, preferably between 15 and 25. The reflux ratio is defined by the ratio of the flow of material reinjected from the head of the column towards the interior of the chamber. the column (ie the reflux rate) and the outflow actually at the outlet of the column head. The feed point of the flow (F2) is chosen in a manner known to those skilled in the art, it is in particular chosen so as to avoid retro-mixtures. Preferably, the feed point is at the top of the depletion section. The ratio of the distillation rate (flow rate (F12)) to the feed rate (flow rate (F2)) is preferably 0.05 to 0.5.

The reflux rate is preferably 1.4 to 3 times the feed rate, for example it is 2 times the feed rate.

Preferably during step b), the bottom temperature of the column is between 100 ° C. and 160 ° C., in particular between 120 ° C. and 150 ° C. Preferably during step b) the temperature at the top of the column is between 80 ° C. and 120 ° C., preferably between 90 ° C. and 110 ° C. The residence time of the vanillin at the bottom of the column of step b) is between 30 minutes and 5 hours, for example it is 3 hours.

Distillation is started by adjusting the flow rate (F12) to maintain a sensible temperature, preferably from 100 to 160 ° C. The temperature difference between the head (vapor temperature) and the foot (liquid temperature) is preferably between 35 and 45 ° C.

To carry out the distillation of step b) the supply of calories at the bottom of the column can be done in particular by a falling-film or scraped-film boiler, by a tube-shell exchanger heated with steam or with a coolant, via heating coils fed with steam or with a heat-transfer fluid or with any other equivalent device, preferably with a heat-transfer fluid. Preferably the energy for the distillation is provided by a falling film type boiler, a forced circulation tube-and-calender or a thermosiphon tube-and-calender. The flow (F13) of the bottom of column at the end of step b) is sent to the distillation column of step c) also called tailing column. Preferably, the column of step c) comprises from 10 to 30 theoretical plates, preferably from 15 to 25 theoretical plates. The distillation column of step c) comprises in particular from 4 to 14 theoretical plates for the depletion section and from 6 to 16 theoretical plates for the concentration section. Preferably the column of step c) is equipped for example with a woven ordered packing. The point of entry of the stream (F13) is between the fifth and fifteenth theoretical plateau from the bottom of the distillation column. In the column of step c), the operating pressure is preferably between 2 and 10 mbar, preferably between 3 and 6 mbar, for example 4 mbar. The pressure drop is preferably from 1 to 10 mbar, preferably from 1 to 8 mbar, for example it is 4 mbar. In step c) the reflux ratio is between 2 and 10, preferably between 2.5 and 6, it is for example 3.

The ratio of the distillation rate (flow rate (F14)) to the feed rate (flow rate (F2)) is preferably 0.5 to 0.95. The reflux rate is preferably 1.4 to 3 times the feed rate, for example it is 2 times the feed rate.

Preferably: the flow rate (F1) is 150 to 220 kg / h; the flow rate of the flow (F11) is from 100 to 180 kg / h; flow rate (F2) is 40 to 55 kg / h; the flow rate of the flow (F12) is 3 to 6 kg / h; the flow rate of the flow (F13) is from 34 to 52 kg / h; the flow rate of the flow (F14) is 20 to 60 kg / h. Preferably during step c), the bottom temperature of the column is between 160 ° C. and 200 ° C., in particular between 170 ° C. and 190 ° C. Preferably, during step c), the temperature at the top of the column is between 100 ° C. and 160 ° C., preferably between 110 ° C. and 140 ° C. The residence time of the vanillin at the bottom of the column of step c) is between 15 minutes and 15 hours, preferably between 30 minutes and 15 hours, more preferably between 7 and 15 hours. In order to reduce this residence time between 15 minutes and 8 hours and to limit the degradation of natural vanillin, which is thermally sensitive, it may be advantageous to add a dead body to the bottom of the column. The dead bodies are well known to those skilled in the art, they may in particular consist of glass beads.

In order to carry out the distillation of step c) the supply of calories at the bottom of the column may be done in particular by a falling-film or scraped-film boiler, by a tube-shell exchanger heated with steam or with a heat-transfer fluid, via heating coils fed with steam or with a heat-transfer fluid or with any other equivalent device, preferably with a heat-transfer fluid. Preferably, the energy for the distillation is provided by a forced circulation tube-and-calender or a scraped heat exchanger. In one embodiment, the process according to the invention makes it possible to obtain a very pure natural vanillin, especially with a purity greater than or equal to 99% and preferably containing less than 1000 ppm of vanillic alcohol. This embodiment can be obtained by adapting the distillation parameters, in particular the ratio of the distillation rate (F14) and the feed rate (F2) is then preferably between 0.67 and 0.734.

In another embodiment, the process according to the invention makes it possible to obtain a natural vanillin of lesser purity, for example of purity of 96 to 98.9%, and comprising impurities conferring on the flow of natural vanillin obtained different organoleptic properties. that of natural vanillin very pure and close to those of the vanilla pod. In this embodiment, the final flow of natural vanillin may comprise up to 3% by weight of impurities. Most of the impurities include vanillic alcohol, and dimers and / or trimers, in particular diphenylmethanes, which can represent up to 1% by weight of the flux, and in the minority vanillic acid, guaiacol, benzoic acid and biosynthesized organic compounds, each of which may be present up to 500 ppm in the stream. This embodiment can be obtained by adapting the distillation parameters, especially the ratio of the distillation rate (F14) and the feed rate (F2) is then preferably between 0.735 and 0.8.

The invention also relates to a device for carrying out this method comprising: a first device for separating (1) ultralights, in particular ethyl acetate, from a stream (F1) entering said first device, this first device being in particular a falling film heat exchanger or a double jacket reactor; - Connecting means of the first device to a first distillation column (2) for transferring the flow from the first device (F2) to the input of said first column; a first distillation column (2) for separating, on the one hand, light substances and, on the other hand, natural vanillin and heavy oils, said first column comprising an inlet of the flow (F2) coming from the first device and an outlet at the top column comprising light (F12), and a columnar outlet comprising natural vanillin and heavy (F13); means for connecting the first column to a second distillation column (3) to transfer the outgoing flow at the bottom of the first column to the inlet of said second column; a second distillation column (3) for separating, on the one hand, natural vanillin and, on the other hand, heavy particles, said second column comprising an inlet of a stream (F13) coming from the first column and an outlet at the top column comprising natural vanillin (F14), and a column bottom outlet comprising heavy (F15).

The device may also contain a pump (4) for transferring the flow from the first device to the first distillation column. The device may also contain a condenser connected to one of the outputs of the first device and making it possible to recover the ultralights and / or a condenser connected to the column head of the column (2) for recovering the light and / or a condenser connected to the column head (3) for recovering the natural vanillin. The characteristics relating to the first device and the distillation columns are specified above. In one particular embodiment, the process carried out by continuous distillation comprises the following steps: a) in a first step, the stream (F1) is treated in order to eliminate the ultra-light (stream (F11)) that it contains and more particularly ethyl acetate, the flow thus obtained comprising natural vanillin, heavy and light is called flux (F2); b) in a second step, the flow (F2) is fed into a first distillation column, to recover at the distillation head a flow (F22) including light and natural vanillin and possibly a low concentration of heavy and full length distilling a stream (F23) comprising the heavy ones, especially vanillic alcohol, and possibly a low concentration of natural vanillin; c) the stream (F22) is supplied continuously in a second distillation column for recovering at the top of distillation a stream (F24) comprising the light and possibly a low concentration of natural vanillin and distillation foot, a stream ( F25) comprising natural vanillin and possibly a low concentration of light and / or heavy. In this embodiment, the term "low concentration" means a concentration of preferably at most 10%, preferably at most 5%, for example at most 3% by weight relative to the total weight of the fraction. According to a preferred embodiment of the tailing / topping scheme, at least a portion of the stream (F23) is mixed with the stream (F25) so as to be able to vary the final composition of a purified natural vanillin stream. Preferably, the flow (F22) at the top of distillation in step (b) comprises the light ones, in particular benzoic acid, guaiacol; natural vanillin and possibly a low concentration of heavy. In bottom of distillation (F23) one finds the heavy ones, in particular the vanillic alcohol and possibly a low concentration in natural vanillin. Those skilled in the art are perfectly able to set the distillation parameters such as, in particular, the diameter of the column, the column height and the packing. We will simply recall the following. The size (especially the diameter) of the distillation columns depends on the circulating flow and the internal pressure. Their sizing will therefore be mainly according to the mixing rate to be treated. It will be specified that the column may be lined with either trays or ordered or woven packing, as is well known to those skilled in the art. The installation being determined, the person skilled in the art adjusts the operating parameters of the column. Preferably, the column of step b) comprises from 10 to 30 theoretical plates, preferably from 15 to 25 theoretical plates. The distillation column of step b) comprises in particular from 4 to 14 theoretical plates for the depletion section and from 6 to 16 theoretical plates for the concentration section. Preferably the column of step b) is equipped for example with a woven ordered packing. The point of entry of the flow (F2) is between the fifth and the fifteenth theoretical plateau from the bottom. In the column of step b), the operating pressure is preferably between 2 and 10 mbar, preferably between 3 and 6 mbar, for example 4 mbar. The pressure drop is preferably 1 to 10 mbar, preferably 1 to 8 mbar, for example it is 4 mbar. In step b) the reflux ratio is between 2 and 10, preferably between 2.5 and 6, it is for example 3. The ratio of the distillation flow rate (flow rate (F22)) on the Feed rate (flow rate (F2)) is preferably 0.5 to 0.95. The reflux rate is preferably 1.4 to 3 times the feed rate, for example it is 2 times the feed rate. Preferably during step b), the bottom temperature of the column is between 160 ° C. and 200 ° C., in particular between 170 ° C. and 190 ° C. Preferably during step b) the temperature at the top of the column is between 100 ° C. and 160 ° C., preferably between 110 ° C. and 140 ° C.

The residence time of the vanillin at the bottom of the column of step b) is between 15 minutes and 15 hours, preferably between 30 minutes and 15 hours and even more preferably between 7 and 15 hours. In order to reduce this residence time between 15 minutes and 8 hours and to limit the degradation of natural vanillin, which is thermally sensitive, it may be advantageous to add a dead body to the bottom of the column. The dead bodies are well known to those skilled in the art, they may in particular consist of glass beads. To carry out the distillation of step b) the supply of calories at the bottom of the column can be done in particular by a falling-film or scraped-film boiler, by a tube-radiator heat exchanger heated with steam or with a coolant, via heating coils fed with steam or with a heat-transfer fluid or with any other equivalent device, preferably with a heat-transfer fluid. Preferably, the energy for the distillation is provided by a forced circulation tube-and-calender or a scraped heat exchanger.

The flow (F22) at the top of the column at the end of step b) is sent to the distillation column of step c), also called the topping column. This stream can be sent in liquid form, the vapors coming from the column of stage b) being totally condensed by means of a condenser, or in vapor form, the vapors coming from the column of stage b) being partially condensed using a partial condenser. Preferably, the stream (F22) is sent to the distillation column of step c) in the vapor phase. This advantageously allows a direct saving of live steam for the distillation column of step c). Thus, the operating pressure of the distillation column of step b) must be greater than that of the distillation column of step c) and a partial condenser is placed between the distillation column of step b) and that of step c). The partial condenser may be any type of condenser known to those skilled in the art, it may be for example a tube-type condenser and calender. Preferably, the flow (F24) at the top of distillation in step c) comprises the light ones, in particular benzoic acid and guaiacol, and optionally natural vanillin in low concentration. Preferably, the distillation column of step c) comprises from 20 to 35 theoretical plates, preferably from 23 to 30 theoretical plates. The distillation column of step b) comprises in particular from 8 to 15 theoretical plates for the concentration section and from 12 to 20 theoretical plates for the depletion section, preferably from 10 to 13 theoretical plates for the concentration section. and from 13 to 17 theoretical plateaus for the exhaustion section. The distillation column c) may be a distillation column equipped with an ordered packing on a height of 2x2600 mm to 2x3000 mm (2600 to 3000 mm for each of the sections of exhaustion and concentration). The lining of the column is preferably a woven lining due to the very low operating pressures. In the column of step c), the operating pressure is preferably between 2 and 10 mbar, preferably between 3 and 6 mbar, for example 4 mbar. The pressure drop is preferably 1 to 10 mbar, preferably 1 to 8 mbar, for example it is 4 mbar. In step c), the reflux ratio is between 10 and 30, preferably between 15 and 25, it is, for example, 20. The feed point of the flow (F22) is chosen in a manner known from FIG. skilled in the art, it is particularly chosen so as to avoid retro-mixtures. Preferably, the feed point is at the top of the depletion section.

The ratio of the distillation rate (flow rate (F24)) to the feed rate (flow rate (F 2)) is preferably from 0.05 to 0.5. The reflux flow rate is preferably 1.4 to 3 times the feed rate, for example it is 2 times the feed rate. Preferably in step c), the foot temperature of column is between 100 ° C and 160 ° C, especially between 120 ° C and 150 ° C. Preferably during step c) the temperature at the top of the column is between 80 ° C. and 120 ° C., preferably between 90 ° C. and 110 ° C.

The residence time of the vanillin at the bottom of the column of step c) is between 30 minutes and 5 hours, for example it is 3 hours. Distillation is started by adjusting the flow rate (F22) to maintain a sensible temperature of 100 to 160 ° C. The temperature difference between the head (vapor temperature) and the foot (liquid temperature) is between 35 and 45 ° C. In order to carry out the distillation of step c), the supply of calories at the bottom of the column can be done in particular by a falling-film or scraped-film boiler, by a tube-radiator heat exchanger heated by steam or by a coolant, via heating coils fed with steam or with a heat-transfer fluid or with any other equivalent device, preferably with a heat-transfer fluid. Preferably the energy for the distillation is provided by a falling film type boiler, a forced circulation tube-and-calender or a thermosiphon tube-and-calender.

Preferably: the flow rate (F1) is 150 to 220 kg / h; the flow rate of the flow (F11) is from 100 to 180 kg / h; flow rate (F2) is 40 to 55 kg / h; flow rate (F22) is 33 to 52 kg / h; flow rate (F23) is 7 to 17 kg / h; the flow rate of the flow (F25) is 20 to 60 kg / h. In one embodiment, the process according to the invention makes it possible to obtain a very pure natural vanillin, especially with a purity greater than or equal to 99% and preferably containing less than 1000 ppm of vanillic alcohol. This embodiment can be obtained by adapting the distillation parameters, in particular the ratio of the distillation rate (F24) and the feed rate (F2) is then preferably between 0.06 and 0.083.35 In another embodiment the process according to the invention makes it possible to obtain a natural vanillin of lesser purity, for example of purity of 96 to 98.9%, and comprising impurities conferring on the flow of natural vanillin obtained organoleptic properties different from that of natural vanillin. very pure and close to those of the vanilla pod. In this embodiment, the final flow of natural vanillin may comprise up to 3% by weight of impurities. Most of the impurities include vanillic alcohol, and dimers and / or trimers, in particular diphenylmethanes, which can represent up to 1% by weight of the flux, and in the minority vanillic acid, guaiacol, benzoic acid and biosynthesized organic compounds, each of which may be present up to 500 ppm in the stream. This embodiment can be obtained by adapting the distillation parameters, especially the ratio of the distillation rate (F24) and the feed rate (F2) is then preferably between 0.084 to 0.1.

The invention also relates to a device for carrying out this method comprising: a first device (1) for separating ultralights, in particular ethyl acetate, from a stream (F1) entering said first device, this first device being in particular a falling film heat exchanger or a double jacket reactor; means for connecting the first device to a first distillation column (5) for transferring the flow (F2) leaving the first device to the inlet of said first column; a first distillation column (5) for separating, on the one hand, light substances and vanillin, and on the other hand heavy materials, said first column comprising an inlet of the flow (F2) coming from the first device and an outlet at the head of column comprising light and natural vanillin (F22), and a column bottom outlet including heavy (F23); - means for connecting the first column to a second distillation column (6) for transferring the flow (F22) outgoing at the head of the first column to the inlet of the second column; a second distillation column (6) for separating, on the one hand, natural vanillin and, on the other hand, light vanillin, said second column comprising an inlet of a stream (F22) coming from the first column and an outlet at the top column comprising the light ones (F24), and an outlet at the bottom of the column comprising the natural vanillin (F25). The device may also contain a pump (4) making it possible to transfer the stream coming from the first device to the first distillation column . The device may also contain a condenser connected to one of the outputs of the first device and for recovering the ultra-light and / or a condenser connected to the column head of the column (6) for recovering light. In the case where the inlet flow of the second distillation column is introduced in the vapor phase, the device also comprises a partial condenser connecting the column head of the first column (5) and the feed point of the second column. (6). In the case where the inlet flow of the second distillation column is introduced into the liquid phase, the device also comprises a condenser connecting the column head of the first column (5) and the feed point of the second column ( 6).

The characteristics relating to the first device, the condenser and the distillation columns are specified above. The embodiment comprising the implementation of a partial condenser allows significant energy savings especially in the context of significant production.

Continuous Column-to-Wall (or DWC) Distillation In one embodiment, the process according to the invention is carried out by continuous distillation using a bulkhead column.

The process carried out by continuous distillation by bulk column comprises the following steps: a) in a first step, the flow (F1) is treated in order to eliminate the ultra-light (flux (F11)) it contains and more particularly ethyl acetate, the resulting stream comprising natural vanillin, light and heavy thus obtained is called flux (F2); b) in a second step, the flow (F2) is fed into a bulkhead column which makes it possible to recover at the top of the column a flow (F32) comprising the light ones and possibly a low concentration of natural vanillin, at the bottom of a column a stream (F34) including heavy, and especially vanillic alcohol, and possibly a low concentration of natural vanillin, the vanillin being recovered in the form of a stream (F33) by lateral withdrawal, this flow possibly comprising a low concentration of light and / or heavy. In this embodiment, the term "low concentration" means a concentration of preferably at most 10%, preferably at most 5%, for example at most 3% by weight relative to the total weight of the fraction. Lateral withdrawal can be carried out in the liquid phase and / or in the vapor phase. This can be done by any method known to those skilled in the art. For example: - in the liquid phase, a packing buffer can be replaced by an overflow recovery tank; in the vapor phase, by a connection with a lateral condenser whose vent pressure is in equilibrium with the head pressure; Advantageously, the lateral withdrawal in vapor phase avoids driving the heavy in the natural vanillin flow obtained. Advantageously, lateral withdrawal in the liquid phase allows an energy saving since the enthalpy subtraction is much less important than a withdrawal in the vapor phase. The vapor phase extraction advantageously makes it possible to increase the purity of the vanillin obtained. The withdrawal in the liquid phase advantageously makes it possible to retain impurities in the final natural vanillin stream, thus making it possible to obtain different organoleptic properties. Advantageously, the process according to the invention may comprise two simultaneous side withdrawals, a lateral withdrawal in liquid and a lateral withdrawal in the vapor phase. This allows in a single distillation step to collect natural vanillin streams of different purity and therefore having different organoleptic properties.

In the context of the present invention, the term "bulkhead column" refers to a distillation column comprising a vertical internal separation segment separating the column into two half-columns of geometry and volume that are independent of each other, a half-column. in which the flow feed (F2) takes place and a secondary half-column in which the flow takes off (F34), the two half-columns communicate with each other, the separation segment not going to one end to the other of the column.

Preferably, the partition column is such that the primary half-column comprises between 18 and 30 theoretical stages, preferably between 25 and 30 theoretical stages, for example 27 theoretical stages; and the secondary half-column comprises between 18 and 25 theoretical stages, preferably between 20 and 25 theoretical stages, for example 23 theoretical stages. Preferably, the primary half-column comprises from 10 to 20 theoretical stages for the depletion section and from 8 to 10 theoretical stages for the concentration section. Preferably, the secondary half-column comprises from 10 to 20 theoretical stages above the vapor phase side draw point and 10 to 15 theoretical stages below the vapor phase withdrawal point. The liquid phase withdrawal is 1 to 4 trays below the vapor phase withdrawal. Preferably, the operating pressure of the bulkhead column is between 2 and 10 mbar, preferably between 3 and 6 mbar, for example 4 mbar. The pressure drop should preferably be identical in each of the two half-columns forming the partition column, for this the diameter of each half-column is adapted. The pressure drop in each half-column is 0.5 to 2.5 mbar. The reflux ratio in each half-column of the same or different partition column is preferably between 2 and 10, preferably between 2.7 and 6. Feeding of the flow (F 2) preferably takes place between tenth and the twentieth theoretical stage of the primary half-column, the trays being counted from bottom to top. The vanillin is withdrawn laterally from the bulkhead column, preferably between the fourth and fifteenth theoretical stage of the secondary half-column, the trays being counted from bottom to top.

Preferably, the separation segment comprises an orifice allowing the passage of a vanillin enriched stream from the primary half-column to the secondary half-column. The orifice is preferably at least two theoretical plates above the feed relative to the primary half-column, preferably it is between 2 and 5 trays above the feed, the trays being counted relative to at the half primary column. The size of the orifice is determined to pass a stream enriched in vanillin and poor in light, the size of the orifice can be determined by the skilled person. It is preferably from 5 to 20 mm, for example from 8 to 15 mm, it is notably about 10 mm wide over the width of the separation segment.

The residence time at the bottom of the column is preferably from 30 minutes to 13 hours, for example 8 hours. In order to reduce this residence time between 1 and 7 hours and to limit the degradation of the natural vanillin, which is thermally sensitive, it may be advantageous to add a dead body at the bottom of the column. The dead bodies are well known to those skilled in the art, they may in particular consist of glass beads.

To carry out the distillation, the supply of calories at the bottom of the column can be done in particular by a falling-film or scraped-film boiler, by a tube-shell exchanger heated by steam or by a heat transfer fluid, by means of coils. heating means powered by steam or a heat transfer fluid or any other equivalent device, preferably a heat transfer fluid.

Preferably, the total side extraction rate ratio (vapor and / or liquid) relative to the flow rate (F2) is 0.5 to 0.95. Preferably: the flow rate (F1) is 150 to 220 kg / h; the flow rate of the flow (F2) is 40 to 70 kg / h; flow rate (F32) is 3 to 7 kg / h; - The flow rate of the flow (F33) in the vapor phase is 20 to 60 kg / h.

When the column has a double vapor and liquid withdrawal, the steam flow rate is 35 to 45 kg / h and the liquid flow rate is 1.0 to 2.5 kg / h. In one embodiment, the process according to the invention makes it possible to obtain a very pure natural vanillin, especially with a purity greater than or equal to 99% and preferably containing less than 1000 ppm of vanillic alcohol. This embodiment is obtained by withdrawing natural vanillin in vapor form. The ratio of the distillation rate (F33) and the feed rate (F2) is then preferably between 0.5 and 0.734. In another embodiment, the process according to the invention makes it possible to obtain a natural vanillin of lesser purity, for example of purity of 96 to 98.9%, and comprising impurities conferring on the flow of natural vanillin obtained different organoleptic properties. that of natural vanillin very pure and close to those of the vanilla pod. In this embodiment, the final flow of natural vanillin may comprise up to 3% by weight of impurities. Most of the impurities include vanillic alcohol, and dimers and / or trimers, in particular diphenylmethanes, which can represent up to 1% by weight of the flux, and in the minority vanillic acid, guaiacol, benzoic acid and biosynthesized organic compounds, each of which may be present up to 500 ppm in the stream. The ratio of the distillation rate (F33) and the feed rate (F2) is then preferably between 0.736 and 0.76.

The process of the invention also makes it possible to obtain, by a single distillation step, the very pure vanillin of purity greater than or equal to 99%, and the vanillin having a purity of 96 to 98.9% by providing two lateral withdrawals, a vapor phase withdrawal to obtain the vanillin purity greater than 99%, and a withdrawal in the liquid phase to recover the vanillin purity 96 to 98.9%. The present invention also relates to a device for carrying out this method comprising: a first device (1) for separating ultralights, in particular ethyl acetate, from a stream (F1) entering said first device, this first device being in particular a falling film heat exchanger or a double jacket reactor; means for connecting the first device to a partition distillation column (7) for transferring the flow leaving the first device (F2) to the inlet of said partition column; a partition distillation column (7) for the separation of light, heavy and natural vanillin, said bulkhead comprising a flow inlet (F2) coming from the first device and a columnar outlet comprising light ( F32), a column bottom outlet comprising the heavy (F34), and one or two side extraction device of the natural vanillin (F33).

The device also contains a pump (4) for transferring the flow from the first device to the partition column. The partition column comprises an inner segment (8) separating the column into two half-columns (71) and (72). The segment comprises an orifice (9) as described above.

The characteristics of the first device and the bulkhead are specified above. The bulkhead method is the preferred embodiment of the invention. In general, in the processes of the invention step a) may be carried out for example by means of a falling film exchanger or a shell reactor (or jacketed reactor), preferably a falling film heat exchanger.

By falling-film evaporator (also called falling-film evaporator) is meant an apparatus consisting of a generally cylindrical chamber comprising a bundle of vertical tubes; said tubes being heated externally by vapor circulation in said chamber. The flow (F1) is supplied by the upper part and falls on a distribution system, for example with a spillway allowing a good distribution of the liquid at the top of the tubes to form a liquid film of a thin thickness, generally less than 1 mm, of preferably between 0.3 and 0.5 mm. During this preliminary step, the operating pressure is preferably atmospheric pressure.

The surface of the exchanger is preferably 0.3 to 0.6 m2 for a feed rate of about 200 kg / h. For a different flow rate the skilled person is able to share his general knowledge of determining the surface of the exchanger. Ultra-light, especially ethyl acetate can be recovered using a condenser for later use.

At the bottom of the falling-film evaporator, a return pump makes it possible to send the liquid stream (F2) recovered at the outlet to the distillation column of stage b), also called a partition column. The flow (F2) corresponds to the flow (F1) substantially or totally free of ultra-light. The stream (F2) may possibly contain ultralight traces that will be trapped in the cold trap of the column of step b).

FIG. 1 represents a continuous distillation scheme for the tipping / tailing of a natural vanillin stream (F1). Figure 2 shows a continuous distillation scheme tailing / topping a natural vanillin flow (F1).

Figure 3 shows a continuous distillation scheme in a bulkhead column of a natural vanillin stream (F1). The present application will now be described using the following examples. The following examples describe the distillation of a vanillin (F1) stream comprising 20% by weight of natural vanillin; 4% by weight of heavy (vanillic acid, vanillic alcohol, ferulic acid, 4-methyl guaiacol, 4 ethyl guaiacol, dimers and trimers, sodium benzoate); 0.5% by weight of water; 2.5% by weight of light (benzoic acid and guaiacol); 73% by weight of ultra-light (ethyl acetate). Example 1: Distillation of the stream (F1) by discontinuous distillation 180 kg of the stream (F1) are fed into the boiler of a distillation column of 700 mm diameter equipped with 10 theoretical trays, lined with a surface woven lining of 450 m2 / m3. The coolant is initially set at 110 ° C and the coolant is a Gilotherm oil at 20 ° C. The column is refluxed for 3 hours. A first fraction comprising ethyl acetate is thus recovered at a flow rate of 15 kg / hour with a reflux of 0.5 for 10 hours. The acetate removal step is complete when the operating pressure is 4 mbar for a heat transfer fluid of 160 ° C. A second fraction comprising light and 10% by weight of vanillin is then recovered at a rate of 2.4 kg / hour with a reflux ratio of 100 for a period of 4 hours.

The column is returned to total reflux for 1 hour when the top temperature reaches 139 ° C., the coolant is set at 165 ° C. for this purpose. A natural vanillin fraction comprising natural vanillin having a purity of 98.2% and a flow rate of 6.1 kg / hour with a reflux of 30 for a period of 10 hours is then recovered. The operating pressure is 4 mbar. After 10h the distillate flow rate is reduced to 3 kg / hour and the reflux ratio is set to 100. The duration of this operation is 0.5 hours. The distillation is stopped when the top temperature reaches 143 ° C, the remaining charge in the pellet is about 9.6 kg and includes the heavy ones. The purification yield is 93%. EXAMPLE 2 Distillation of Stream (F1) by Continuous Distillation Top / Tailing Example 2 refers to Figure 1.

The flow (F1) is fed at a rate of 200 kg / hour at the top of a falling film exchanger (1). This exchanger makes it possible to eliminate the ethyl acetate under a stream (F11) at a flow rate of 146 kg / hour. The flow (F11) is sent to a condenser (not shown) for recovery of ethyl acetate. A flow (F2) is recovered at the outlet of the evaporator which corresponds to the flow (F1) substantially free of ethyl acetate. The traces of ethyl acetate present in the stream (F2) are recovered in the cold trap of a distillation column (2) thereby protecting the column (2). The flow (F2) is sent to a distillation column (topping) (2) via a recovery pump (4), partially recycled, at the rate of 54 kg / hour. At the top of the column (2), a flow (F12) at the rate of 5 kg / hour comprising benzoic acid, gaiacol and 3% by weight of vanillin is recovered.

At the bottom of the column (2), a flux (F13) comprising the heavy metals and the remaining natural vanillin which is sent to a tailing column (3) at a rate of 49 kg / hour are recovered. Column head (3) is recovered a stream (F14) of natural vanillin comprising 3% by weight of heavy consisting essentially of vanillic alcohol and dimers, including diphenylmethane, at a rate of 40 kg / hour. The purity of the vanillin is equal to 97%. The yield of the process is 97%. At the bottom of column (3) is recovered a flow (F15) heavy and 3% by weight of natural vanillin at a rate of 9kg / hour. The characteristics of the device are the following: - Exchanger (1): Surface = 0.5 m2. - Column (2) Equipped with an ordered packing (woven at low speed) on a height of 2x2600m m 24 theoretical trays divided into 11 trays for the section of concentration and 13 trays for the section of exhaustion Column of 4 meters in height Operating pressure: 4 mbar. Reflux rate: The column is first classified for 5 hours with a vanillin mixture (90% by weight), benzoic acid (10% by weight). The distillation is then started by adjusting the flow rate (F12) to maintain a sensible temperature of 140 ° C. The temperature difference between the head (vapor temperature) and the foot (liquid temperature) of 39.6 ° C under 4 mbar. The column is in total reflux for the classification phase.

The energy for distillation is provided by a falling film type boiler, a forced circulation tube-and-shell or a thermosiphon tube-and-shell. - Column 3 Equipped with an ordered woven surface covering approximately 450 m2 / m3, on a height of 2x4560 mm The feeding point is at the Z dimension = 1500 mm 18 theoretical plates Diameter of 600 mm Operating pressure: 4 mbar The column is refluxed with a pure vanillin foot previously melted in an oven. Reflux ratio: 3 Ratio [distillate flow rate] / [feed rate] is 0.808 temperature between the head (vapor temperature) and the foot (liquid temperature) is 43 ° C under 4 mbar.

The energy for the distillation is provided by a tube-and-calender with forced circulation or a scraped heat exchanger. The calender side pressure is 16 bar. EXAMPLE 3 Distillation of the Stream (F1) by Continuous Distillation Tacking / Topping Example 3 refers to FIG. 2. The stream (F1) is fed at the rate of 198.26 kg / hour at the top of a film exchanger. falling (1). This exchanger makes it possible to eliminate the ethyl acetate under a stream (F11) at a flow rate of 147 kg / hour. The flow (F11) is sent to a condenser (not shown) for recovery of ethyl acetate.

A flow (F2) is recovered at the outlet of the evaporator which corresponds to the flow (F1) substantially free of ethyl acetate. The traces of ethyl acetate present in the stream (F2) are recovered in the cold trap of a distillation column (5) thereby protecting the column (5). The flow (F2) is sent to a distillation column (tailing) (5) via a recovery pump (4), partially recycled, at the rate of 51.26 kg / hour. At the bottom of the column (5), a flux (F23) comprising heavy and 3% by weight of vanillin is recovered. At the top of the column (5), a flux (F22) is recovered at a flow rate of 44 kg / hour, comprising the light ones, the remaining vanillin and 2.5% by weight of heavy which is sent to a topping column (6) at flow rate of 44kg / hour. Column head (6) is recovered a stream (F24) comprising light and 3% by weight of vanillin. At the bottom of column (6) is recovered a stream (F25) of natural vanillin comprising vanillin and 2.5% by weight of heavy at a rate of 38.6 kg / h. The vanillin obtained has a purity of 99.9% and the purification yield is 98.9%.

The characteristics of the device are the following: - Exchanger (1): Surface = 0.5 m2. - Column (5) Equipped with an ordered woven lining of approximately 450 m2 / m3 surface, on a height of 2x4560 mm The feeding point is on the Z scale = 1500 mm 18 theoretical plates Diameter of 600 mm Working pressure : 4 mbar Reflux ratio: 3 Ratio [distillate flow rate] / [feed rate] is 0.83 Reflux flow rate is 2.49 times the feed rate Temperature difference between the head (vapors temperature) and the foot (temperature of the liquid) is 26 ° C under 4 mbar The energy for the distillation is provided by a tube-and-calender with forced circulation or a scraped heat exchanger. The calender side pressure is 12 bar. - Column (6) Equipped with an ordered packing (woven at low speed) on a height of 2x2600m m 24 theoretical trays divided into 11 trays for the section of concentration and 13 trays for the section of exhaustion Column of 4 meters in height Operating pressure: 4 mbar. Reflux rate: The column is first classified for 5 hours with a vanillin mixture (90% by weight), benzoic acid (10% by weight). The distillation is then started by adjusting the flow rate (F24) to maintain a sensible temperature of 140 ° C. The temperature difference between the head (vapor temperature) and the foot (liquid temperature) of 35 ° C under 4 mbar. The column is in total reflux for the classification phase. The energy for the distillation is provided by a falling film type boiler, a forced circulation tube-and-shell or a thermosiphon tube-and-calender. The calender side pressure is 10 bar. An alternative is to feed the column (6) in the vapor phase: it uses for this partial condensation via a partial condenser. This alternative is a direct saving of live steam for the column (6). The column (5) then operates at 5 mbar; the column (6) remaining at 4 mbar. In this case, the head temperature reads 139 ° C. The partial condenser comprises a control loop LIC which controls the flow of reflux. The total steam flow to the boiler is controlled by slaving the thermal load to the boiler at the pressure drop of the column OP = 3 mbar). The condenser is a horizontal tube-and-grille comprising 80 tubes; of DN10 (DN: Nominal Diameter in mm) and length 1150 mm. The coolant is Gilotherm oil at 85 ° C and flow rate 533 L / h. The set liquid height of the LIC is 165 mm. This emergence makes it possible to obtain 44 kg / h of vents for 176 kg / h of vapor phase which enters the condenser. The calibrated vent valve of the condenser is set at 5 mbar (opening if> 5 mbar). The flow of live steam at the inlet of the column (6) is regulated so as to ensure a pressure drop of 3.3 mbar. EXAMPLE 4 Flow Distillation (F1) on a Partition Column with Vapor Retraining Example 4 refers to FIG. 3. The flow (F1) is fed at the rate of 200 kg / hour at the top of a heat exchanger. falling film (1). This exchanger makes it possible to eliminate the ethyl acetate under a stream (F11) at a flow rate of 147 kg / hour. The flow (F11) is sent to a condenser (not shown) for recovery of ethyl acetate.

A flow (F2) is recovered at the outlet of the evaporator which corresponds to the flow (F1) substantially free of ethyl acetate. The traces of ethyl acetate present in the stream (F2) are recovered in the cold trap of a distillation column (7) thereby protecting the pump from the column. The flow (F2) is sent to a distillation column (7) at a rate of 53 kg / hour. The following are recovered: a stream (F32) comprising light and 3% by weight vanillin at a flow rate of 5 kg / hour at the top of the column; - A stream (F33) in lateral withdrawal including vanillin with a purity of 98.9% and 1.1% by weight of heavy essentially consisting of vanillic alcohol at a rate of 39 kg / hour. The yield of the purification process is 96.5%; - A flow (F34) at the bottom of the column comprising heavy and 3% by weight of vanillin at a rate of 8 kg / hour. The characteristics of the device are the following: - Exchanger (1): Surface = 0.5 m2. - Column (7) Partition column equipped with a partition segment (8) delimiting a primary half-column (71) and a secondary half-column (72) - an ordered packing of specific surface 450 m2 / m3 in the half primary column (71) at a height of 5410 mm and an ordered packing in the half-secondary column (72) at a height of 4560 mm The primary half-column has a number of stages of 27 The secondary half-column has a number of stages of 23 The operating pressure: 4 mbar The reflux ratio: 3 in each half-column.

A passage (9) in the segment (8) to the dimension 3110 mm enriches the concentration section of the 2nd half-column. The opening of the passage is a band that does not exceed 10 mm wide A difference in temperature between the foot and the head of 74.9 ° C when the head temperature is around 116 ° C.

The reflux flow rate of the downstream section represents 2.18 times the feed rate (F2) and that of the upstream section represents 25% of the feed rate (F2). The set pressure drop is 1.3 mbar for the column. The energy for the distillation is provided by a scraped film type boiler or a forced circulation tube-and-calender.

EXAMPLE 5 Distillation of Flow (F1) on a Wall Column by Vapor / Liquid Double Stripping Example 5 refers to Figure 3 to which is added an additional liquid draw point. The flow (F1) is fed at a rate of 200 kg / hour at the top of a falling film exchanger (1). This exchanger makes it possible to eliminate the ethyl acetate under a stream (F11) at a flow rate of 147 kg / hour. The flow (F11) is sent to a condenser for recovery of ethyl acetate.

A flow (F2) is recovered at the outlet of the evaporator which corresponds to the flow (F1) substantially free of ethyl acetate. The traces of ethyl acetate present in the stream (F2) are recovered in the cold trap of a distillation column (7) thereby protecting the pump from the column. The flow (F2) is sent to a distillation column (7) at a rate of 53 kg / hour. The following are recovered: a stream (F32) comprising light and 3% by weight vanillin at a flow rate of 5 kg / hour at the top of the column; a side vapor withdrawal stream (F33) comprising vanillin with a purity of 99.8% and 0.2% by weight of heavy material consisting essentially of vanillic alcohol at a flow rate of 38.2 kg / hour; - a stream (F35) (not shown) in liquid phase side withdrawal comprising vanillin with a purity of 98% and 2% by weight of heavy at a flow rate of 1.7 kg / hour; - A flow (F34) at the bottom of the column comprising heavy and 3% by weight of vanillin at a rate of 8 kg / hour. The overall yield of the purification is 98.5%.

The characteristics of the device are the following: - Exchanger (1): Surface = 0.5 m2. - Column (7) Partition column equipped with a partition segment (8) delimiting a primary half-column (71) and a secondary half-column (72) - an ordered packing of specific surface 450 m2 / m3 in the half primary column (71) at a height of 5410 mm and an ordered packing in the secondary half-column (72) at a height of 4560 mm The primary half-column has a number of stages of 27 The secondary half-column has a number of stages of 23 The operating pressure: 4 mbar The reflux ratio: 3 in each half-column. A passage (9) in the segment (8) to the dimension 3110 mm enriches the concentration section of the 2nd half-column. The opening of the passageway is a strip not exceeding 10 mm wide. Lateral withdrawal in the vapor phase is located 1200 mm from the base of the packing bed. Lateral withdrawal in the liquid phase is located 400 mm below the side withdrawal in the vapor phase. A difference in temperature between foot and head of 74.9 ° C when the head temperature is around 116 ° C. The reflux flow rate of the downstream section represents 2.18 times the feed rate (F2) and that of the upstream section represents 25% of the feed rate (F2). The set pressure drop is 1.3 mbar for the column. The energy for the distillation is provided by a scraped film type boiler or a forced circulation tube-and-calender.

Claims (14)

CLAIMS 1. A process for purifying a stream (F1) derived from a process for producing natural vanillin, said stream (F1) comprising natural vanillin and at least vanillic alcohol, said process comprising the distillation of said stream (F1) allowing the separation of natural vanillin from vanillic alcohol and the recovery of a distilled natural vanillin stream. 2. A process according to claim 1, wherein the distilled natural vanillin has a purity greater than or equal to 99%. 3. A process according to any one of claims 1 or 2, wherein the operating pressure during the distillation is between 2 and 10 mbar, preferably between 3 and 6 mbar. 4. Method according to any one of claims 1 to 3, wherein the pressure drop during the distillation is between 1 and 10 mbar. 5. A process according to any one of claims 1 to 4, wherein the flow (F1) comprises from 5 to 35% by weight of natural vanillin; from 0.05 to 10% by weight of vanillic alcohol; from 0.0 to 2% by weight of vanillic acid; from 0.0 to 2% by weight of ferulic acid; from 0.0 to 2% by weight of guaiacol; from 0.0 to 5% by weight of dimers and trimers; from 0.0 to 5% by weight of various organic compounds which are also biosynthesized; from 0.0 to 10% by weight of benzoic acid; from 0.0 to 5% by weight of water; the complement at 100% by weight being a food solvent. 6. A process according to one of claims 1 and 3 to 5, wherein the distilled natural vanillin has a purity of 96 to 98.9%. 7. A process according to claim 6, wherein among the impurities are predominantly vanillic alcohol, and dimers and / or trimers, especially diphenylmethanes, which represent up to 1% by weight of the flow, and in the minority vanillic acid, guaiacol, benzoic acid and biosynthesized organic compounds, each of which is up to 500 ppm. 8. A process according to any one of claims 1 to 7, wherein the flow (F1) is loaded into a distillation column and are recovered: - in a first fraction ultra-light; in a second fraction the light ones; in a third fraction natural vanillin; and - in the distillation pellet the heavy ones. 9. A process according to any one of claims 1 to 7 comprising the following steps: a) in a first step, the flow (F1) is treated in order to eliminate the ultra-light it contains and more particularly the ethyl acetate (F11), the flux thus obtained is called flux (F2); b) in a second step, the flow (F2) is fed into a first distillation column, to recover at the distillation head a flow (F12) comprising the light and foot distillation a flow (F13) including natural vanillin and heavy ones; c) the flow (F13) is supplied continuously in a second distillation column for recovering at the distillation head a stream (F14) comprising natural vanillin and at the bottom of a distillation stream (F15) comprising the heavy. 10. A process according to any one of claims 1 to 7 comprising the following steps: a) in a first step, the stream (F1) is treated in order to eliminate the ultra-light it contains and more particularly the ethyl acetate (F11), the flux thus obtained is called flux (F2); b) in a second step, the flow (F2) is fed into a first distillation column, to recover at the top of a distillation stream (F22) comprising light and natural vanillin and at the bottom of a distillation stream (F23) including heavy, and especially vanillic alcohol; c) the flow (F22) is supplied continuously in a second distillation column for recovering at the distillation head a stream (F24) comprising the light and bottom distillation, a stream (F25) comprising natural vanillin. 11. A process according to any one of claims 1 to 7, comprising the following steps: a) in a first step, the stream (F1) is treated in order to eliminate the ultra-light that it contains and more particularly the ethyl acetate, the flux thus obtained is called flux (F2); b) in a second step, the flow (F2) is fed into a bulkhead column which makes it possible to recover at the top of the column a flow (F32) comprising the light ones, at the bottom of the column the heavy ones and in particular the vanillic alcohol, the vanillin being recovered in the form of a stream (F33) by lateral withdrawal in the vapor or liquid phase or in the form of two streams respectively by lateral withdrawal in the vapor phase and by lateral withdrawal in the liquid phase. 12. A device, in particular for carrying out the process according to claim 9, comprising: a first device for separating ultralights, in particular ethyl acetate, from a flow entering said first device, first device being in particular a falling film exchanger or a jacketed reactor; - means for connecting the first device to a first distillation column for transferring the flow from the first device to the inlet of said first column; a first separation distillation column on the one hand, and vanillin and heavy ones on the other, said first column comprising an inlet of the stream coming from the first device and a columnar outlet comprising the light ones, and a exit at the bottom of the column including natural vanillin and heavy; means for connecting the first column to a second distillation column to transfer the outgoing flow at the bottom of the first column to the inlet of the second column; a second separation distillation column, on the one hand natural vanillin and on the other hand light ones, said second column comprising an inlet of a stream coming from the first column and a columnar outlet comprising natural vanillin , and an output at the bottom of the column including the heavy ones. 13. A device, in particular for carrying out the process according to claim 10, comprising: a first device for separating ultralights, in particular ethyl acetate, from a stream entering said first device, first device being in particular a falling film exchanger or a jacketed reactor; - means for connecting the first device to a first distillation column for transferring the flow from the first device to the inlet of said first column; a first separation distillation column, on the one hand, light and vanillin, and, on the other hand, heavy said first column comprising an inlet of the stream coming from the first device and an outlet at the top of the column comprising the light and the natural vanillin, and an exit at the bottom of the column including the heavy ones; means for connecting the first column to a second distillation column in order to transfer the outgoing flow at the top of the first column to the inlet of the second column; a second separation distillation column, on the one hand natural vanillin and, on the other hand, light ones, said second column comprising an inlet of a stream coming from the first column and a top-of-column outlet comprising the light ones, and an outlet at the bottom of the column comprising natural vanillin. 14. Apparatus for carrying out the method according to claim 11 comprising: a first device for separating ultralights, in particular ethyl acetate, from a flow entering said first device, said first device being in particular a falling film heat exchanger or a double jacket reactor; means for connecting the first device to a partition distillation column for transferring the flow from the first device to the inlet of said partition column; a distillation column with a separating partition for light, heavy and natural vanillin, said partition column comprising an inlet of the stream coming from the first device and a columnar outlet comprising light, an outlet at the bottom of the column; comprising the heavy, and a lateral withdrawal device of the natural vanillin vapor phase or liquid phase or two lateral withdrawal devices respectively vapor phase and liquid phase.