JPS581913B2 - Method and apparatus for producing fermented beverages with reduced alcohol content - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method and apparatus for reducing the alcohol content of fermented beverages such as beer, wine, and Sekt by dialysis.

For various reasons, research has been conducted for several years to produce fermented beverages such as beer, wine, and sekt with reduced alcohol content.

One of the reasons for this is the maximum blood alcohol concentration of motor vehicle drivers, which makes it desirable to produce beverages with reduced alcohol content.

Another important reason is that diabetics can consume fully fermented beverages, which are dangerous for diabetics due to their higher alcohol content than normally fermented beverages. Beer generally consists of the following 3 types:
Two types must be distinguished: 1. Beer with reduced alcohol content to 2-3% by weight, 2. The alcohol content, which is called low alcohol beer, is 1
．． Beer reduced to 5% by weight or less; 3. Beer with an alcohol content of 0.5% by weight or more is called alcohol-free beer.

Beer with a reduced alcohol content has so far been produced in fundamentally different ways, either by selection of the manufacturing method or by post-treatment of conventionally produced phorbier (raw wort 11-14%).

The scope of the first method includes the reduction of the original wort, the regulation of a low final fermentation degree and the use of low-fermenting yeast.

Beer that has not been completely fermented must necessarily have a different taste depending on the degree of fermentation, and unfermented or early-fermented wort can provide a special taste, but beer produced by reducing wort (the so-called Shank beer (raw wort 7-8%) tastes watery.

When post-processing normally fermented beer, the desired amount of alcohol is removed from the produced beer by distillation at atmospheric pressure, vacuum distillation or reverse osmosis.

Furthermore, selective separation of alcohols using adsorption resins and freezing methods has also been proposed.

Distillation at atmospheric pressure results in a product with a markedly altered taste due to protein alteration, increased content of hydroxymethylfurfurol and a number of unspecified high temperature reactions of various beer-containing substances. Although the phenomenon can be reduced by the use of vacuum distillation, it cannot be completely avoided.

This is because beer is still accompanied by an unfavorable change in bitter substances with an increase in temperature, even if only slightly.

Until now, methods similar in principle to those that have become known in particular for beer have also been applied in research on producing other fermented beverages such as wine, fruit wine or sekt with reduced alcohol content.

The method closest to the present invention is the separation of alcohol by reverse osmosis.

Such a reverse osmosis method is described in West German Published Patent Application No. 213593.
No. 8, No. 2243800, No. 2333094, and 2 more
409609 and 2415917.

For example, German Published Patent Application No. 2135938 proposes the production of alcohol-free or low-alcohol beer by reverse osmosis using cellulose acetate membranes or nylon membranes. It can be generated by a plunger pump.

The disadvantages of the method described here are obvious: firstly, not only alcohol but also water is removed from the beer, so that the beer concentrated in this way can be subsequently diluted with water or used to produce normally fermented plain beer ( (2-5.5%) to the desired alcohol content and adjust the initial or desired raw wort.

However, such a method inevitably impairs the sense of taste.

Secondly, in order to carry out the method proposed here high system pressures and high membrane differentials are required in all cases, the supply is pulsating despite the provision of an air tank; Therefore, pressure fluctuations within the system and differential pressure fluctuations across the membrane occur.

Therefore, the major drawback of reverse osmosis is the beer side, which has about 30 to 50
is at a high system pressure of atii, and this pressure has a pressure of 4at.
The dialysate pressure of ii must be counteracted.

The high differential pressures that occur, of more than 25 bar, lead to great equipment difficulties and, in addition to the alcohol, also remove most of the water from the beer.

Therefore, a special method of refeeding water to the beer is required, as the above-mentioned publication shows.

The object of the present invention is to reduce the alcohol content of conventionally produced fermented beverages such as beer, wine, sekt, etc. to a desired degree without any particular deterioration in the taste of the beverage.

This object is solved by a method in which a fermented beverage produced by a conventional fermentation process is guided along a dialysis membrane with a differential pressure of less than 5.0 bar, and at the same time the dialysate flows on the other side of the dialysis membrane.

Differential pressure refers to the pressure difference between the two sides of the membrane.

During dialysis, material exchange occurs almost exclusively by diffusion, so
Although the extent of mass exchange is determined by the concentration gradient across the membrane, in reverse osmosis the pressure differential plays an important role and this pressure differential must be significantly greater than the osmotic pressure.

According to the method of the invention, osmotic pressure is not necessarily reached; the differential pressure is generally lower than 1.0 bar.

A differential pressure of less than 0.5 bar is particularly advantageous; the process can also be carried out almost without a differential pressure.

In addition to the above-mentioned reasons, the deterioration in taste in the case of the known method is also due to the fact that together with the alcohol or alcohol-water mixture, a portion of the low-molecular-containing substances, such as the extract, is likewise removed.

According to reverse osmosis, separation of low molecular weight substances is unavoidable unless the membrane has excellent selectivity.

If the selectivity of the membrane is too low, a portion of the low molecule-containing substances, ie the extract, will pass through the membrane wall along with the alcohol.

According to the formulation of the invention, therefore, the dialysate contains a fermented beverage extract in a suitable concentration to prevent the passage of the beverage extract.

For this purpose, it is possible to use alcohol-free fermented beverages produced by any method and corresponding to the beverages to be dialyzed.

For example, when producing beer with reduced alcohol content, alcohol-free beer can be used as the dialysate.

When using an extract-containing dialysate, it is particularly advantageous to remove the alcohol enriched in the dialysate by means of the other forms according to the invention from the dialysate by adsorption, extraction, reverse osmosis and/or distillation.

The alcohol-free dialysate can be used cyclically as a dialysate, which is particularly advantageous in order to prevent the passage of the extract through the membrane, since an equilibrium state is reached very quickly.

In the case of carbon dioxide-containing fermented beverages, the process is carried out at high system pressures, but the differential pressure is kept very small to avoid ultrafiltration.

The pressure at which the dialysis is carried out is above the saturation pressure of the carbon dioxide dissolved in the fermented beverage, so that the carbon dioxide remains dissolved at the surface of the membrane, or the carbon dioxide remains dissolved as it passes through the membrane. Gas cushion formation is avoided.

For example, the amount of carbon dioxide lost during production cannot be added back to Sekt later.

This is possible in the case of beer, but in fermented beverages
It would be advantageous if the carbon oxide could be completely dissolved and retained.

For this purpose, an amount of carbon dioxide corresponding to the amount of carbon dioxide in the fermented beverage to be dialyzed is dissolved in the dialysate.

Thereby, a reduced-alcohol fermented beverage containing a normal amount of carbon dioxide is passed through the dialyzer and can be stored in a conventional manner.

In addition to dialysis, it is often advantageous to ultrafiltrate fermented beverages.

By adjusting the differential pressure, the ultrafiltration rate can be adjusted very precisely.

Conventional dialysis membranes with ultrafiltration rates of about 2-5 ml/m hmmHg are capable of ultrafiltration in very fine stages and limited to the desired degree.

Particularly if a slightly higher ultrafiltration is desired, this additional ultrafiltration, according to the formulation of the invention, can be carried out at an ultrafiltration rate of 7 to 3
Performed by a dialysis membrane with an ultrafiltration rate of 0 ml/m h mmHg (7).

Such a membrane is described in German patent application P2823985,5.

Additional ultrafiltration can also be achieved by increasing the differential pressure by 0.5 to 5.0 bar.

If dialysis is often carried out at elevated pressures from 0.5 to 1.0 bar and/or at elevated differential pressures, ultrafiltration is already sufficient to achieve the desired taste improvement. be exposed.

Particularly when a solution of a particular composition (including an extract) is used as the dialysate, it is advantageous to carry out the ultrafiltration in a separate ultrafiltration step from the dialysis step.

Since in the case of fermented beverages there is a risk of extract loss during the dialysis process, it is advantageous to follow the dialysis process with a separate ultrafiltration process.

Allowing limited ultrafiltration in addition to dialysis has been demonstrated to be effective in improving the quality of wines, especially those with reduced alcohol content.

Many wines, for example due to unfavorable weather conditions, lose their extract content, resulting in a watery taste.

In this case, the method according to the invention results in not only a reduction in alcohol but also a marked improvement in taste.

In the case of Sekt and beer, ultrafiltration can be carried out in a similar manner in addition to dialysis if necessary.

Furthermore, it is an object of the present invention to avoid the above-mentioned drawbacks of the known art and to create an apparatus which is suitable not only for the production of low or alcohol-free beer, but also for reducing the alcohol content of other fermented beverages such as wine, sekt and other conventional alcohol-containing beverages. It's also about getting.

This purpose according to the invention comprises a separation membrane unit which is at least one dialysis membrane, a first chamber connected to a first supply conduit and a first discharge conduit, and a second chamber connected to a second supply conduit and a second discharge conduit. , a casing containing the membrane, the two chambers being separated from each other by the membrane and customary liquid-impermeable sealing elements and partitions; a supply device operating at uniform pressure, coupled to the first and second chambers; one each for the first and second supply conduits and/or the first
and a flow controller placed in each of the second discharge conduits for regulating a constant low differential pressure between the first and second chambers. The invention is solved by a device having a controller for regulating the pressure level, a device for regulating the temperature of the liquid flowing through the first chamber and/or the second chamber.

Dialysis hollow systems and dialysis tubes or sheets are demonstrated as suitable membranes for use in the device of the invention, which can be arranged in the device in a straight or planar or curved manner. .

Particularly suitable membranes for the apparatus of the present invention are membranes that can be produced by regenerating cellulose from a cuprammonium cellulose solution.

Particularly good results are obtained with the device of the invention when the membranes used have a low permeability for molecules with a molecular weight of more than 100, in which case membranes with as high a selectivity as possible, i.e. as sharp a separation limit as possible, are advantageous. be.

The advantage of membranes with sharp separation limits is that they allow almost only alcohol to pass through the membrane, while other low-molecular-containing substances, such as sugars, bitter substances, aroma substances, etc., pass through the membrane to a much lesser extent or not at all. be.

Another advantage provided by this dialysis membrane is that high differential pressures across the membrane are not required, as is the case, for example, in reverse osmosis, in order to separate alcohols with high selectivity.

The first and second portions generally correspond to the differential pressure acting on the membrane.
Particularly good results are achieved using such a membrane in the device according to the invention when the differential pressure between the chambers is very low.

Particularly good results are obtained when the pressure difference is below 0.1 bar, and good results can also be achieved with a pressure difference of 0.5 bar and even up to 5.0 bar.

In order to set the most suitable differential pressure in each case on the membrane, the device according to the invention therefore includes control mechanisms in the first and second supply and/or discharge conduits that are as sensitive as possible depending on the operational requirements. Placed.

It has proven particularly advantageous for the membrane to be present in the form of a membrane unit that is releasably connected to the casing.

This type of implementation allows the membrane to be replaced by another membrane in a simple manner, ie by exchanging the entire unit.

In order to obtain a compact structure, ie a large exchange area for a small space, hollow fiber modules in which the membrane consists of a large number of hollow fibers have proven particularly advantageous.

The hollow fibers may in this case be present in the form of linear hollow systems running approximately parallel to each other or, for example, in the form of regular and/or irregular loops, spatially extending coils and/or thousand-sided spirals. The hollow fibers are arranged in multiple layers such that the hollow fibers of each layer intersect with the hollow fibers of each adjacent layer, possibly multiple times, and the open ends of the hollow fibers are placed in the casting material so that the hollow fibers can freely pass through the hollow fibers. It can be embedded in such a way that it does not obstruct passage.

The cross-sectional shape of the membrane module is arbitrary. In particular, the casing housing the dialysis membrane, the supply and discharge conduits, the sealing elements, the partitions, the supply device and the control organs characteristic of the device of the invention, which are present in the form of modules, can be manufactured from all customary metal or non-metallic materials. In the selection of materials, at least for the liquid contacting parts of the device of the invention, attention must be paid to the laws and regulations applicable to the food industry.

The selection of the various components of the device of the invention is generally based on the dimensions of other devices and mechanisms used in the respective factory or on the dimensions commonly used in industry.

According to the mode of implementation of the device according to the invention, chosen at a working pressure suitably higher than atmospheric pressure, a reduction in the alcohol content of the liquid maintains a favorable differential pressure across the separation membrane for the separation problem to be solved in each case. However, it can advantageously be carried out at a pressure such that no sudden evolution of dissolved carbon dioxide occurs at atmospheric pressure, such as occurs in the case of sekt, or saturation occurs, as occurs in the case of beer.

An embodiment of the device according to the invention, which is designed for a nominal pressure 16, generally meets normal working requirements in many cases.

However, this device can advantageously also be adapted to high pressures.

Taking into account the uniform quality of the beverage to be treated and the possible uniform separation capacity of the membrane as well as the advantageous low differential pressure across the membrane, the supply of the liquid to be treated, i.e. the beverage or beverage product, and the alcohol-absorbing liquid, i.e. the dialysate, can be easily controlled. It has turned out to be advantageous for the supply to be uniform and not pulsating or impulsive in any case.

For the supply of both liquids along the membrane surface, pumps which meet this requirement are suitable, for example, and supply devices which operate only under static pressure without moving parts have proven particularly suitable for this purpose.

Such a supply device may consist, for example, of a liquid container in which a uniform liquid level is regulated or maintained by known means and mechanisms.

In order to increase the static pressure, such containers can be constructed in a closed construction and additionally be connected to a compressed gas line in order to create a compressed gas cushion above the container liquid level.

It has proven particularly advantageous to use oxygen-free gases for this purpose, in particular carbon disilide and/or nitrogen.

By using such a gas, oxygen destruction or other deterioration of the liquid to be treated, which often occurs already on contact with air, is advantageously avoided.

The advantage of such a dosing device is not only that there are no moving parts that can cause wear, but also that the liquid is fed quietly and in an air-tight manner, without air oxygen, undesired wear particles of the pump or pump seals, etc. reaching the liquid. I'm in the middle of something.

A particularly uniform flow rate per unit time can be achieved with such a supply device in conjunction with a flow control device that operates with very high precision.

In order to guarantee a constant flow rate over time, for example, so-called throttle holes have proven particularly suitable.

Variations in the flow rate through the throttle openings are possible in a known manner, for example, by varying the prepressure.

If it is desired to be able to vary the flow rate with a uniform prepressure, it is possible according to the invention to use a so-called needle valve as the flow control device.

This is because this valve allows very fine flow rate adjustments and at the same time guarantees a single flow rate adjustment over a long period of time.

The flow control device can be arranged before and/or after the casing in which the separation membrane is arranged.

Furthermore, other suitable constant flow control devices commonly used in industry for this purpose can also be used, as long as they satisfy the respective requirements for a constant flow rate as far as possible in time.

The control device has a drive, such as electric, pneumatic or hydraulic, which can be connected to a customary measuring and control device, so that the flow rate can be automatically monitored, controlled and optionally adjusted. , or desired flow rate changes can be implemented remotely.

The same applies to adjusting and changing the liquid level or gas cushion pressure of the supply device.

For example, if a constant flow ratio of beverage to dialysate is desired, the respective flow control devices are advantageously coupled together such that a change in the volume of one fluid changes the volume of the other by a predetermined ratio.

It is likewise advantageous to provide in advance a quantity ratio that depends on the flow rates of the two liquids, which automatically occurs when one of the two flow rates changes.

In order to maintain the liquid to be processed, such as a finished or semi-finished beverage, at a temperature below room temperature, the production according to the invention comprises a temperature regulating device for the liquid passing through the first and/or second chamber.

Such a device, in the simplest case, i.e. when the liquid to be treated is already precooled, is an insulating device for all or at least one part of the device according to the invention.

However, by the use of conduits, containers and other equipment parts with heating or cooling jackets, temperature regulation of the liquids can also be achieved with respectively heated or cooled fluids, in which case the two liquids are heated or cooled before and/or after treatment. It can also be brought to different temperature levels.

When treating liquids such as Sekt in which gases, e.g. Accordingly, a gas addition device, in particular a carbon dioxide addition device, is arranged at least in the first or second supply conduit and/or in the first or second discharge conduit.

Such a device makes it possible, for example, to dissolve in the treatment liquid, ie, the dialysis liquid, an amount of gas corresponding to the gas previously dissolved in the liquid to be treated, thereby avoiding said diffusion of gas through the membrane.

Another method of compensating for the loss of gas dissolved in the liquid to be treated consists in additionally dissolving a corresponding amount of gas only in the liquid to be treated, so that the liquid has the desired gas content after treatment. .

Finally, it is also possible to add the gas amount of the treated liquid lost due to the treatment with the dialysis membrane only after the treatment.

A combination of these three exemplified methods is also conceivable.

The suitability of either of the above methods can be easily determined by individual experimentation, or is often influenced by existing regulations, ordinances, laws, etc. In particular, the dissolution of the carbon dioxide is particularly advantageously carried out in a container formed in the closed structure of the supply device.6 In this case, the device according to the invention allows all of the air and oxygen of the liquid thus loaded to be dissolved. Contact is advantageously prevented, ensuring uniform and quiet dispensing of the liquid,
A gas pressure cushion is created which is necessary for the adjustment of arbitrarily high pressure levels and the dissolution of gas into the liquid.

It is also advantageous to charge the liquid with a gas mixture, for example a mixture of nitrogen and carbon dioxide.

For this purpose, additional gas connections can be provided at appropriate locations or a gas mixture of the desired composition can already be supplied.

Such a method of operation is very advantageous, for example, when a high gas pressure cushion is required, but only an amount of gas corresponding to a low partial pressure must be dissolved in the liquid.

This method of operation also offers significant advantages, in particular when higher pressures, which correspond to the partial pressure of the carbon dioxide dissolved in the sect, have to be set for the gas pressure cushion, for example.

In this case, if the gas cushion consists only of carbon dioxide, additionally an unacceptable amount of carbon dioxide will be dissolved in the gas.

On the other hand, for example, in the case of a gas cushion made of pure nitrogen,
Even at pressures exceeding the partial pressure of the carbon dioxide dissolved in the Sekt, the carbon dioxide escapes from the Sekt by diffusion into the nitrogen atmosphere.

Depending on the type and scale of the work and the hourly flow rate of the liquid to be treated by the device according to the invention, other configurations according to the invention may optionally include a large number of dialysis membrane modules, each housed in one suitable casing. It is expedient to use small dialysis membrane units connected in parallel, so that only one fraction of the total flow rate can be conducted through each module, which can optionally be adjusted by suitably arranged controls.

Such a device allows each individual module to be replaced during operation of the device according to the invention, possibly without having to interrupt the operation of the entire device during replacement, or is equipped with a considerable number of spare modules. If necessary, it is possible to switch to this reserve module without interruption or reduction of the total flow rate.

A series connection of two or more membrane modules is advantageous, for example, if the alcohol content of the liquid is to be reduced in stages, possibly even to near-zero values.

In order to regulate and monitor the once-adjusted flow rate, known flow measuring devices can advantageously be placed at any position in the respective supply and/or discharge conduit.

When using a large number of parallel-connected membrane modules, it has proven highly advantageous to provide each module with a suitable flow meter and a suitable control arrangement.

The direction of flow of both liquids along the surface of the membrane can be co-current, counter-current or cross-current depending on the formation of the device according to the invention.

For example, combinations such as orthogonal one-way flow or orthogonal one-current flow are also possible.

Which of the many methods is best is case-specific and often determined by the preferred flow diameter for mass exchange, as well as fluidics considerations or, as in the case of the present invention, e.g. influenced by the requirement for the lowest possible pressure differential at the surface.

Next, the present invention will be explained with reference to the drawings.

The embodiment of the device according to the invention shown in FIG. 1 has a separation membrane 1 formed in the form of a unit arranged in a casing 3;
A flange 2 arranged on the end face of the casting material of the membrane unit, together with a sealing ring 5 and a partition 4 of the housing 3, separates the second chamber 7 of the housing 3 from the first chamber 6 in a liquid-impermeable manner.

Since the membrane unit is in this case releasably connected to the casing 3, the membrane unit can be removed after removing one or both of the end wall members 45, which are releasably connected to the casing wall via the seals 46, and unit can be replaced.

The first chamber 6 is connected to a first supply conduit 8 and a first discharge conduit 9, and the second chamber 1 is connected to a second supply conduit 10 and a second discharge conduit 11.

The first supply conduit 8 is a first supply device 12 which operates only under static pressure.
The second supply conduit 10 is likewise connected to a second supply device 22
connected to.

The two supply devices 12 or 22 each have a closed liquid 14 or 24, a liquid supply conduit 15 or 25, a liquid overflow pipe 16 or 26 for always adjusting the liquid level 17 or 27 to the same level, and a liquid overflow pipe 16 or 26 above the liquid level 17 or 27. Gas supply pipe 1 for creating a gas pressure cushion 19 or 29 in
Consisting of 8 or 28 gas cushions 19 or 29
The pressure is measured and monitored by a pressure gauge 13 or 23.

Furthermore, two supply conduits 8 and 10 are connected via a shutoff device 21 or 31 to a gas supply pipe 20 or 30.

Both supply conduits 8 are used to control the hourly flow rate of the liquid to be treated, i.e. beverage, and the liquid to be treated, i.e. dialysate.
Alternatively, a flow rate measuring device 32 or 35 is arranged at 10.

Two control valves 33 and 36 connected to a common controller 38 serve to regulate the flow rate, the first chamber 6 and the second chamber 7
A pressure measurement and controller 34 or 37 is used which is combined with the same controller 38 in order to monitor the lowest possible pressure difference between.

In the discharge conduit 11 or 9 there is in each case a control valve 39 or 41 connected to a controller 43 and a pressure measuring and controller 4.
0 or 42 is placed.

The two controllers 38 and 43 may also be coupled to each other or form one unit.

With such a circuit it is possible to set within a wide range the desired pressure level at a given flow rate in the two chambers 6 and T and at the same time the desired pressure difference, which is generally as low as possible across the separation membrane.

If desired, the casing 3 can further be surrounded by an insulating wall 44.

Additionally, the conduits and equipment may also be insulated or temperature controllable conduits and/or equipment may be used.

However, the entire device according to the invention can also be placed in a suitably temperature-controlled room.

In the first part, no operational equipment is shown that is connected before or after the device of the invention, depending on the task.

FIG. 2 shows a parallel connection of four membrane modules 1, each arranged in one casing 3, with other parts as shown in FIG. 1 of this embodiment of the device according to the invention not being apparent from the drawing. Not shown for purposes of illustration.

Each module has its first supply and discharge conduit 8 or 9
connected to a common first main supply conduit 49 or first main discharge conduit 50 by a second supply and discharge conduit 1
0 or 11 to a common second main supply conduit 41 or second main discharge conduit 48.

In order to control and measure the possibly different magnitudes of the sub-flows passing through each individual module, each supply conduit 8 or 10 and/or each discharge conduit 9 or 11 is provided with a suitable measuring and measuring system, for example as shown in FIG. A control or regulator may be provided.

The main supply conduits 47 and 49 are each connected to a supply device, not shown.

The method of the invention will now be illustrated by the alcohol reduction of beer as shown in the following example.

In the case of wine, sekt, fruit wine, sake, and other fermented beverages, it is possible to obtain a fermented beverage with a reduced alcohol content and which is palatable without changing the method.

Example I Starting from a known beer belonging to the beer marketed under the trademark Pils.

With a raw wort content of 12%, Pils has an alcohol content of 3.91
% by weight and extract content of 3.93%.

Baus, which is commonly used at Kozo Kogyo, is used to determine the alcohol content.
ch, Billig; Silber-Eisen (Ve
"Arbeitsvorschriften Zu" by Paul Baney 1963)
r Chemisch-Brautechnische
The test was carried out by the method described on page 101 of ``N Betriebskontrolle''.

Determination of extract content is similar to “Arbei tsvorsc”
Hriften zur Chemisch-Brau
technischenBetriebskontro
The same method as described on page 101 of "Ille" was carried out by a method commonly used at Kozo Kogyo.

Corresponding hollow fiber membrane dialysis units are well known in hemodialysis, using dialysers as membranes with bundles of cellulose hollow fibers spun from cellulose cuprammonium solution for dialysis.

The exchange area of the hollow fiber membrane was 1.3 m.

Beer was introduced at a rate of 30 l/h-m through the hollow fiber at a temperature of 10 DEG C. and a system pressure of 4 bar, and water at the same temperature as immediately after dialysis was introduced onto the outer surface of the hollow fiber.

The differential pressure was 0.05 bar and the beer had high pressure.

After reaching equilibrium, a beer with a 30% reduction in alcohol content was obtained, with the extract content decreasing by only about 10%.

Taste tests revealed that a pils was obtained which was quite comparable in taste to the original beer used.

The amount of beer passed without changing the amount of dialysate was approximately 1. /3 a 65% reduction in alcohol content is achieved and a beer is thus obtained which can already be called a low alcohol beer.

It is clearly more enriched in taste than beer of the same alcohol content produced by known methods.

If the dialysate contains beer extract, the taste is of course comparable to the starting beer.

When producing so-called alcohol-free beer, ie beer with an alcohol content of approximately 0.5% by weight, this is achieved by further reducing the throughput of beer by a factor of 2 without changing the dialysate volume.

In this case as well, if beer extract is added to the dialysate, beer with better taste can be obtained.

Example 2 Beer with the same characteristic values as Example 1 was exchanged with an area of 1.3 m''
The samples were dialyzed at 10° C. in a hollow fiber dialyzer with various liquid flow rates.

Starting from a raw wort content of 12%, an alcohol content of 3.91% and an extract content of 3.93%, the analytical values shown in the following table were obtained after dialysis.

Example 3 Wine was dialyzed in a similar manner in a hollow fiber dialyzer with an exchange area of 1.3 m' (corresponding to Examples 1 and 2).

Wine was introduced through the hollow fiber at a system pressure of 4 bar and a temperature of 10° C., and completely demineralized water was introduced as a dialysate at the same temperature onto the outer surface of the hollow fiber.

The differential pressure is in this case 0.05 bar (or 0 in experiment d
．． 5 bar), the wine had high pressure.

The characteristic values of the dialyzed wine are shown in the following table.

The alcohol content of the wine used was 6.7. 9g/
The L extract content was 20.59/t and the acid content (calculated as grape acid) was 6.85 g/l.

Example 4 In the same dialyzer and under the same conditions, the alcohol is removed in each case by vacuum distillation from the dialysate after passing through the dialyzer,
The solution volume was replenished with completely demineralized water and used as a new dialysate.

In this case, alcohol 80.8g/l, extract 21.2g
/l and acid 8.2 g/l wine.

Completely demineralized water was used as the initial dialysate.

The results of the dialyzed wine obtained up to equilibrium in one pass are evident from the following table.

The differential pressure was 0.15 bar in this experiment.

Example 5 Two steel casings each with an exchange area of 1.9 m''
Two dialyzers were connected in series for sparkling wine (Sekt) dialysis.

The alcohol was removed by vacuum distillation, Sekt, diluted to original volume with fully demineralized water and saturated with carbon dioxide, was used as the dialysate.

The system pressure was 4.7 bar.

The pressure difference at the outlet was 0.20 bar and the temperature was 10°C.

Zect was introduced through the dialyzer at a rate of 1.394/h-m, and the dialysate was applied to the other side of the membrane at a rate of 1.394/h-m. 3 8 4/h
− led at a speed of m.

The alcohol content of Sekt was reduced to 89.2% by dialysis.
g/l to 51.3 g/l.

The extract content of 22.3 g/l and the acid content of 9.4 g/l remained unchanged in this case.

The taste was completely equivalent to commercially available Sekt.

In order to carry out a further series of experiments, the apparatus of the present invention corresponding to the first embodiment was used, and five
It was possible to selectively switch to the previous hollow fiber units.

The arrangement of the units corresponded to the circuit shown in FIG. 2, and the size and exchange area (membrane area) of the individual units were the same.

Each unit was placed in its own casing.

The amount of liquid passing through each unit could be adjusted individually, ie independently of each other, by means of a measurement and control or regulator provided in each unit.

All units were connected to one main conduit in each case of the liquid to be treated (beverage) or dialysate.

In this case the beverage flowed through the hollow fibers and the dialysate flowed around them.

Experiments were carried out with various beers known under the trademarks K2;lsch, Pils, Export and Di:it.

Completely desalinated water was used as the dialysate.

Example 6 Replacement area of each of 5 hollow fiber units Approx. lm Number of hollow fibers per hollow fiber unit // 10000 Thickness of hollow fiber (film thickness) 〃11 μm Diameter of hollow fiber
Ultrafiltration rate of 200 μm hollow fiber: 4 mA/h·m′·mmHg The hollow fiber was fixed in a plastic casing in the form of a bundle of substantially parallel fibers with casting resin.

Beer flow rate per unit 1: 6.3 to 63 l/h Dialysate flow rate per unit: 6.3 to 63 l/h Beer or dialysate temperature: approx. 10°C Maximum control pressure on beer side (absolute): approx. 4 bar Dialysis Maximum adjustment pressure on liquid side (absolute)
approx. 3.95 bar differential pressure
Alcohol content of beer before 0.05 bar treatment 17-4.7% Alcohol content of beer after treatment
17-3.0% Example 7 Replacement area of each of the five hollow fiber units Approximately 6 m Number of hollow fibers per hollow fiber unit Approximately 40,000 Beer passing amount per each unit 40-400 l/h Dialysate passing amount per each unit 4 0- Other data and values for all 400 l/h were as in Example 6.

The hollow fibers were arranged in each case in the form of a hollow fiber module which was releasably connected to a special steel casing.

[Brief explanation of drawings]

FIG. 1 is a functional explanatory diagram of the device of the present invention, and FIG. 2 is a diagram showing the connections of the devices of the present invention arranged in parallel. 1...Separation membrane, 3...Casing, 4
...Bulkhead, 5...Seal, 6...
...1st room, 7...2nd room, 8,10...
... Supply conduit, 9, 11... Discharge conduit, 12,
22... Supply device, 14, 24... Liquid container, 18, 20, 28, 30... Gas supply pipe, 33, 36... Flow rate control Valve, 34, 37,
40.42... Pressure measurement and controller, 38
．． 43...Controller, 39,41...
Control valve, 44...Insulating wall.

Claims (1)

[Claims] 1. A method for producing fermented beverages such as beer, wine, and Sekt with reduced alcohol content, in which a fermented beverage produced by a conventional fermentation method is passed along a dialysis membrane at a pressure difference of less than 5.0 bar. 1. A method for producing a fermented beverage with reduced alcohol content, characterized in that the dialysate is guided on the other side of the dialysis membrane and at the same time the dialysate is allowed to flow on the other side of the dialysis membrane. 2. The method according to claim 1, wherein the differential pressure between the fermented beverage and the dialysate is less than 1.0 bar. 3. A method according to claim 1 or 2, wherein the pressure difference between the fermented beverage and the dialysate is less than 0.5 bar. 4. Process according to one of claims 1 to 3, wherein the differential pressure between the fermented beverage and the dialysate is less than 0.1 bar. 5. The method according to one of claims 1 to 4, wherein the dialysis membrane has a low permeability to molecules with a molecular weight of 100 or more. 6. The method according to one of claims 1 to 5, wherein the dialysate contains an extract of a fermented beverage. 7. The method according to claim 6, wherein an alcohol-free fermented beverage corresponding to the beverage to be dialysed, produced by any method, is used as the dialysis fluid. 8. In the case of a fermented beverage containing carbon dioxide, the method according to one of claims 1 to 7, wherein the pressure at which the dialysis is performed is higher than the saturation pressure of carbon dioxide dissolved in the fermented beverage. 9. The method according to claim 8, wherein the dialysate contains carbon dioxide in an amount corresponding to the amount of carbon dioxide in the fermented beverage to be dialyzed. 10. A method for producing fermented beverages such as beer, wine, and sekt with reduced alcohol content, in which a fermented beverage produced by a conventional fermentation method is guided along a dialysis membrane at a pressure difference of less than 5.0 bar and simultaneously dialyzed. Method for producing fermented beverages with reduced alcohol content, characterized in that a dialysate is passed through the other side of the membrane, in which case the fermented beverage is subjected to dialysis and additionally ultrafiltration, 11. Ultrafiltration as a dialysis process 11. The method according to claim 10, which is carried out in a separate ultrafiltration step. 12. The method of claim 11, wherein a separate ultrafiltration step is connected after the dialysis step. 13 Additional ultrafiltration using dialysis membranes from 7 to 30 m
13. The method according to claim 10, wherein the method is carried out at an ultrafiltration rate of l/m hmmHg. 14. The method according to one of claims 10 to 13, wherein the dialysis membrane has a low permeability to molecules with a molecular weight of 100 or more. 15. The method according to one of claims 10 to 14, wherein the dialysate contains an extract of a fermented beverage. 16. The method according to claim 15, wherein an alcohol-free fermented beverage corresponding to the beverage to be dialysed, produced by any method, is used as the dialysis fluid. 17. In the case of a fermented beverage containing carbon dioxide, the method according to one of claims 10 to 16, wherein the pressure at which the dialysis is performed is higher than the saturation pressure of carbon dioxide dissolved in the fermented beverage. 18. The method according to claim 17, wherein the dialysate contains carbon dioxide in an amount corresponding to the amount of carbon dioxide in the fermented beverage to be dialyzed. 19 In a method for producing fermented beverages such as beer, wine, and sekt with reduced alcohol content, a fermented beverage produced by a conventional fermentation method is guided along a dialysis membrane at a pressure difference of less than 5.0 bar, and at the same time the dialysis membrane is A method for producing a fermented beverage with a reduced alcohol content, characterized in that the alcohol enriched in the dialysate is removed from the dialysate by adsorption, extraction, reverse osmosis and/or distillation. . 20. The method according to claim 19, wherein a dialysate from which alcohol has been removed is used as the dialysate. 21. In the case of a fermented beverage containing carbon dioxide, the method according to claim 19 or 20, wherein the pressure at which the dialysis is performed is higher than the saturation pressure of carbon dioxide dissolved in the fermented beverage. 22. The method according to claim 21, wherein the dialysate contains carbon dioxide in an amount corresponding to the amount of carbon dioxide in the fermented beverage to be dialyzed. 23. In an apparatus for producing fermented beverages such as beer, wine, and Sekt with reduced alcohol content, the first chamber 6 and the second supply conduit 10 are connected to the dialysis membrane unit 1, the first supply conduit 8, and the first discharge conduit 9. and a second chamber 7 connected to a second discharge conduit 11, these two chambers 6,
and a supply operating at homogeneous pressure that connects the casing 3 containing the membrane 1, the first chamber 6 and the second chamber 7, separated from each other by a conventional liquid-impermeable sealing element 5 and/or a partition 4. devices 12, 22, flow controllers 33, 36 arranged one each in the first and second supply conduits 8, 10 and/or one each in the first and second discharge conduits 9, 11, a first chamber; 1 between 6 and 2nd room 7
Controller 34.37 for adjusting the constant low differential pressure. 3
8. Controls 39, 40, 4 for adjusting any power levels in the two chambers 6, 7 that differ at most at most little;
1, 42, 43. An apparatus for producing a fermented beverage with reduced alcohol content, characterized in that it has a device 44 for adjusting the temperature of the liquid flowing through the first chamber 6 and/or the second chamber. 24. Device according to claim 23, in which the feeding device 12.22 operates solely under static pressure without moving parts. 25. Device according to claim 24, in which the at least one supply device 12, 22 has a liquid storage container 14.24 charged with an inert gas. 26. Device according to one of claims 23 to 25, in which the membrane unit 1 is present in the form of a membrane module 1 to 3 that is fluid-tight but releasably connected to the casing 3. 2T In an apparatus for producing fermented beverages such as beer, wine, and Sekt with reduced alcohol content, the first chamber 6 and the second supply conduit 10 are connected to the dialysis membrane unit 1, the first supply conduit 8, and the first discharge conduit 9. and a second chamber 7 connected to a second discharge conduit 11, these two chambers 6,
and a supply operating at homogeneous pressure that connects the casing 3 containing the membrane 1, the first chamber 6 and the second chamber 7, separated from each other by a conventional liquid-impermeable sealing element 5 and/or a partition 4. devices 12, 22, flow controllers 33, 36 arranged one each in the first and second supply conduits 8, 10 and/or one each in the first and second discharge conduits 9, 11, a first chamber; 1 between 6 and 2nd room 7
controller 34 for adjusting the constant low differential pressure; 37
．． 3B, a controller 39,4 for adjusting the arbitrary pressure levels in the two chambers 6.7 that differ at most only slightly;
0, 41, 42, 43, with a device 44 for adjusting the temperature of the liquid flowing through the first chamber 6 and/or the second chamber, at least the first or second supply conduit 8, 10
and/or an apparatus for producing a fermented beverage with reduced alcohol content, characterized in that a carbon dioxide addition device 20, 21, 30, 31 is arranged in the first or second discharge conduit 9, 11.