RU2694324C2 - Compact reactor for enzymatic treatment - Google Patents

Abstract

FIELD: biotechnology.

SUBSTANCE: disclosed is a reactor for enzymatic hydrolysis of material. Reactor successively includes a first heat exchanger for heating raw material to facilitate enzymatic hydrolysis of temperature, reaction chambers, as well as a second heat exchanger for heating reaction mixture to temperature exceeding the range of promoting enzymatic hydrolysis of temperatures. At that, reaction chambers are arranged at different in vertical levels, where first reaction chamber is uppermost, and the last reaction chamber is the lowest one, wherein at least one of the reaction chambers is made for mixing of its content with the inert gas passing through the chamber.

EFFECT: invention ensures stable reaction conditions for the supplied material irrespective of changes in external conditions.

22 cl, 8 dwg

Description

The present invention relates to the type of reactor, which is described in the preamble of paragraph 1 of the claims.

BACKGROUND

When conducting, for example, enzymatic processing of organic materials in order to carry out their hydrolysis (decomposition), to achieve the desired result, it is necessary to adjust the temperature of the material and the duration of the effect of enzymes on the material (duration of contact). Too long or too short contact time adversely affects the product obtained in the process and may cause problems with additional processing of the material and / or adversely affect the quality of the finished product obtained in the manufacturing process. Thus, the main task is to establish the proper duration of the contact.

When using industrial enzymes for hydrolysis or other enzymatic processing, suitable enzymes are added to the raw material. After the addition and distribution of enzymes in the raw material, it is important to ensure that the mixture is constantly stirred to establish sufficient contact between the enzyme and the raw material. As noted above, it is important that the enzymes are in contact with the raw material for a certain period of time. Thus, it is important that after this time interval the enzymatic decomposition is quickly stopped, and the process does not go too far. Usually the process is stopped by heating the mixture of raw material and enzymes to a temperature at which the enzymes are destroyed (inactivated).

Similar problems can arise in a number of other chemical methods, where it is important to obtain a homogeneous mixture of components, and it is also important to control the duration of the reaction, which should not significantly exceed or be less than the optimal duration if it is necessary to obtain a final product of the required quality.

The simplest way to achieve the required contact duration is to use batch reactors that work with “batches” of material. In batch devices, a certain volume (tank or similar capacity) is kept under certain conditions for a certain time, and then the process is terminated. As already noted, additional enzyme heating is used in enzymatic methods to inactivate the enzyme. In industrial production, large volumes are processed, which are difficult to heat quickly enough if they are treated as a batch. The alternative is to process multiple batches of small volume, but this leads to a disproportionate increase in production costs.

Intermittent methods have other disadvantages as compared to continuous methods, regardless of whether these methods include enzymatic treatment. One of these drawbacks is much more frequent start and stop of the method. It is labor intensive, and such methods are more difficult to automate than continuous methods. In addition, the operating conditions during start-up and shutdown are usually more unstable than is acceptable.

The goal is to create a continuous stream of homogeneously mixed raw material, and the processes occurring in the material must be inactivated during a certain time interval. Passing a continuous stream of raw materials through a large container in which "full mixing" takes place is not a good solution, since in this case it is very difficult to control the duration of contact between the individual components.

The reactor for enzymatic processing of the raw material is discussed in Norwegian patent No. 322996 (WO 2006/126891). The treatment is carried out in a substantially vertical reactor with separate reaction chambers, the material in each chamber being mechanically agitated using a stirrer and transferred to the adjacent chamber below under the action of gravity. The reactor provides suitable retention times and suitable conditions for all materials being processed.

In particular, for the processing of raw materials of marine origin, it is important that the processing on board begins as soon as possible after the catch. Thus, it is important that the processing takes place in compact equipment, the properties of which are not too affected by the excitement at sea, which causes the ship to roll.

OBJECTIVES OF THE INVENTION

The object of the present invention is to provide a system and / or reactor for the hydrolysis of the raw material, in which stable reaction conditions can be ensured for the whole feed material, regardless of changes in external conditions.

The object of the present invention is also to provide a reactor that combines the advantages of periodic methods and continuous methods in cases where the duration of contact between the components is a critical parameter on which the quality of the product depends.

Another objective of the present invention is to achieve the above objectives using a convenient and inexpensive method implemented on an industrial scale.

A specific object of the present invention is to provide a reactor for the hydrolysis of raw material of marine origin on board a ship, i.e. in a limited space in which stable reaction conditions can be maintained at different wind strength and waves.

SUMMARY OF INVENTION

The above problems can be solved by creating a reactor according to claim 1 of the claims. Preferred embodiments of the invention are disclosed in the dependent claims.

The material processed in the reactor can be called both a “raw material” and a “material”.

The reactor according to the present invention can be manufactured as a compact device, and the external reactor can be in the form of a cylinder placed in front, in which the reaction chambers are arranged with a given inclination relative to the horizontal plane, while the reactor as a whole is oriented essentially vertically. The reaction chambers are tubular in shape and preferably have a circular cross section; exceptions are presented in the attached graphic materials and their discussion. The inclination of each camera may be different, but preferably it is at least 1/10 (vertical / horizontal ratio) [5.7 degrees]. In some embodiments, the slope may be 1/5 [11.3 degrees].

The required heat transfer can be carried out in a concentric direction with and within the vertical coil of the reaction chambers. Stirring is carried out by bubbling inert gas through the reaction chambers. Valves installed between all reaction chambers provide the same residence time in each reaction chamber and, thus, the same total residence time in the reactor. Transportation of partially processed material from one reactor compartment to the next can be accomplished by creating an overpressure of inert gas used for mixing in the corresponding reaction chamber by closing the valve upstream in the chamber and opening the valve downstream.

Below the invention is discussed in more detail with reference to the following accompanying graphic materials.

FIG. 1 is a perspective view of a first embodiment of a reactor according to the present invention.

FIG. 2 schematically shows one of the reaction chambers according to one of the embodiments of the present invention.

FIG. 3 is a schematic sectional view of certain details of the embodiment shown in FIG. one.

FIG. 4 is a schematic representation of the other details of the embodiment shown in FIG. one.

FIG. 5 is a schematic block diagram of a method in which a reactor according to the present invention is used.

FIG. 6 is a schematic and simplified top view of the reactor shown in FIG. one.

FIG. 7 is a schematic and simplified top view of a reactor according to the present invention, which is one embodiment of the reactor shown in FIG. one.

FIG. 8 is a side view of another embodiment of the reactor according to the present invention.

FIG. 1 generally shows one of the embodiments of the reactor according to the present invention. The reaction chambers R1-R6 are spirally arranged from top to bottom in the form of a reactor, about which it can be said that, in general, it is oriented vertically or along a vertical axis. A randomly selected reaction chamber may be indicated by Ri, where i is a numerical value. Along the circumference, the size of each of the reaction chambers R is close to 360 degrees, that is, to the full circle. After each of the reaction chambers Ri, a valve Vi is installed, where i is the numerical value separating it from the next chamber. Thus, after the reaction chamber R1 valve V1 is installed. In the present embodiment, the valves V1-V5, which separate the chambers from each other, are placed one above the other. This is done for convenience and is not an essential feature of the reactor. In the present embodiment, below the reaction chambers are three pasteurisation chambers P1-P3, having essentially the same shape and size as the reaction chambers. Pasteurization chambers are also separated by valves designated VP1 and VP2. The exact number of reaction chambers and pasteurization chambers may vary.

FIG. 1 also shows the feed line 01 for the raw material and the discharge line 02 for the material being processed. Also presented are: an inert gas tank 13 capable of withstanding pressure, an inert gas pipe 10 leading to each of the reaction chambers and pasteurization chambers, a waste inert gas collector 11 and a return pipe 14 for recycling the waste inert gas to the container 13 through the compressor 12. Inert gas is released from the reaction chambers through valves having the general designation RVi (where i is a numerical value). Three such valves are indicated in FIG. 1 as RV1-RV3.

In addition, in FIG. 1 shows an air supply pipe 03 supplying air to at least one heat exchanger and an air discharge pipe 04 discharging from a heat exchanger designated HEX2. In practice, two heat exchangers are commonly used, as discussed in more detail below.

FIG. 1 also shows a pipeline 17 for the material being processed leading from the reaction chamber R6 to the heat exchanger HEX2. Also shown is a pipe 16 connecting the upper part of the heat exchanger HEX2 to the inlet of the pasteurization chamber P1. FIG. 1 also shows a part of the pipeline 18 through which the raw materials, which have already passed heat exchange, are fed into the reaction chamber R1.

FIG. 2 shows a cross-section of a single reaction chamber, and chamber 3 was chosen randomly. The difference from the embodiment shown in FIG. 1 is that, for simplicity, the reaction chamber is represented as a straight chamber. The design of the reactor according to the present invention may also include straight chambers. The material is fed into the reaction chamber R3 through the valve V2, shown in the right part of the image, while the release of material is carried out through the valve V3, shown in the left part of the image. The slope of the reaction chamber facilitates the movement of material by gravity. FIG. 2, the slope of the reaction chamber is approximately 1/10. In practice, this is often sufficient, but in some cases the slope may be greater, for example, be 1/5. An inert gas, usually nitrogen, is injected through a supply line 10 connected to the downstream end of the reaction chamber and discharged through an outlet 21 located near the end of the upstream reaction chamber. During processing, both valves V2 and V3 are closed, that is, for a limited period of time, the material remains stationary in the reaction chamber. As shown by arrows, the movement of inert gas through the chamber causes the material to circulate in the chamber. Thus, inert gas is used to effectively mix the treated mass. On the inlet pipe 10, connected to the reaction chamber, the inlet valve IV3 is installed, and on the outlet pipe 21 for gas, connected to the collector 14, the return valve RV3 is installed.

When the reaction chamber 3 is to be emptied, the valve RV3 is closed and an overpressure of a selected value is created in the reactor. It is important that both valves V2 and V3 are also closed. It is assumed that the adjacent downstream reaction chamber R4 was previously released from the material, and excessive pressure was released in it. The valve V3 is then opened, which leads to a rapid release of pressure as the gas and the material moves into the reaction chamber R4, and this movement is also facilitated by the action of gravity. While the gas is distributed between the two chambers in question, essentially all solid and liquid materials end up in the reaction chamber 4, in which further processing will take place.

It should be understood that the reaction chamber R3 was chosen randomly and for example only; essentially the same type of treatment is carried out in all reaction chambers, and the main reason for using such a number of separate chambers is to ensure the same residence time for the entire mass being processed; at the same time, the flow of material observed from the outside, from the inlet of the reaction chamber R1 to the outlet of the reaction chamber R6, moves in a mode close to full displacement. The flow of material discharged from the reaction chamber R6 is somewhat different, since it is not directed directly to the lower chamber, but directed to a heat exchanger for further heating in order to stop the hydrolysis reaction. The temperature of the suspension at the outlet of this heat exchanger can usually reach 90 ° C or more.

It should be clear to a person skilled in the art that in a situation where all the reaction chambers are filled with the material being processed, the reaction chamber R6 must be freed from the material until any other chamber is empty, and the reaction chamber R5 must be freed from the material before the emptying of the reaction chamber R4 , etc. However, to release the space for placing the material removed from the reaction chamber R6, it is necessary to carry out the same procedure with pasteurization chambers P1-P3, that is, release the chambers P3, P2 and P1 in the specified order.

The heat transfer according to the present invention is carried out in a substantially classical manner, i.e. it can be carried out in the same manner and in the same equipment as in the methods according to the prior art. However, from the point of view of space saving and for other reasons, it is preferable that the heat exchange takes place in a heat exchanger installed coaxially with respect to the reaction chambers, that is, they are arranged in such a way that together they form a spiral.

FIG. 3 shows a cross section in the vertical direction of the heat exchange system, which may form an integral part of the present invention. The image shows the reaction chambers R1-R6, as well as pasteurization chambers P1-P3. Coaxially with respect to them and to the vertical axis of the reactor, two heat exchangers HEX1 and HEX2 are located one above the other, which can also be considered as one two-stage heat exchanger. The task of the lower heat exchanger HEX1 (or the lower stage of the heat exchanger) is to heat the material to a temperature that favors the flow of enzymatic hydrolysis, usually to a temperature of approximately 50 ° C. This is done by feeding the material stream to the reactor through the supply line 01 (Fig. 1), before the material enters the reaction chamber R1. In the present embodiment, the material flow delivered to the HEX1 heat exchanger is passed through the supply conduit 01 upward through the HEX1 heat exchanger through a coil 33 laid in the form of a spiral near the outer wall of the heat exchanger. Heat is supplied to the heat exchanger using the heat exchange device 31. Usually, the heat exchanger HEX1 is filled with a liquid, preferably an aqueous liquid. In addition, in the present embodiment, air is supplied to the heat exchanger from the air source 03 through the collector 35. The air causes the water to move upward in the central part of the heat exchanger, while the water flows downwards, circulating, along the peripheral part of the heat exchanger, in which the spiral coil 33 is located; thus, with respect to the coil 33, the heat exchange is essentially carried out in countercurrent mode.

Next, FIG. 4, and also FIG. 3. The outlet of the coil 33 is connected to the pipeline 18 (FIG. 4), through which the heated raw material is fed to the reactor R1. The typical temperature of the mixture of materials supplied to the reactor R1 is 50 ° C, but it may differ from the indicated temperature by several degrees in any direction. To regulate the opening of the valve of the heat exchange installation 31, a real, measured in real time value of the temperature of the material into the reactor R1 or at the outlet of the coil 33 can be used.

The heat exchanger (or heat exchange stage) HEX2 has the same general design as the heat exchanger HEX1. The material treated in reactors R1-R6 is sent to the heat exchanger HEX2, to the coil 34 laid upwardly upward, which is placed near the heat exchanger wall, through pipe 17. A sufficient amount of heat is supplied to the heat exchanger HEX2 via heat exchanger 32. that the material passed through the coil 34, is heated to a temperature sufficient to stop the enzymatic hydrolysis. A suitable temperature may be about 90 ° C or more. To regulate the opening of the damper of the heat exchange installation 32, a real, measured in real time value of the material temperature at the exit of the coil 34 can be used. The material extracted from the HEX2 heat exchanger is sent to the first pasteurization chamber P1 through the pipe 16.

For a more visual demonstration of the external connections of the pipeline, in FIG. 4 shows the details of the reactor 1, from which the reaction chambers and pasteurization chambers were removed. The image shows: pipeline 01 for feeding material, pipeline 02 for the material being processed, pipelines 03 and 04 for supplying air to the heat exchanger and extracting air from the heat exchanger, respectively, pipeline 17 for moving material from the reaction chamber R6 (Fig. 1) to the second heat exchanger HEX2, pipe 18 for transferring material from the first heat exchanger HEX1 to the first reaction chamber R1 (Fig. 1), and pipeline 16 for moving the material from the second heat exchanger HEX2 to the first pasteurization chamber P1 (Fig. 1).

It should be particularly noted that the heat exchangers described in the present description are only an example of a suitable arrangement of heat exchangers, and for the purposes of the invention any heat exchanger can be used, allowing the raw material to be heated to a temperature that contributes to the flow of enzymatic hydrolysis, and any heat exchanger that can be heated to higher temperature, ensuring the termination of enzymatic hydrolysis of the material. However, it is preferable to use an available volume for heat exchange, located along the axis of a vertically installed reactor, and the presented principle of creating a spiral circuit for moving material and air bubbling through heat exchangers is convenient because they provide good temperature distribution in heat exchangers and in practice essentially countercurrent heat exchange due to the action air, which draws fluid up in a volume close to the vertical axis of the heat exchangers, after what the liquid flows down on the peripheral parts of the heat exchangers.

FIG. 5 is a flow diagram of a method in which an installation according to the present invention is used, shown in the embodiment shown in FIG. 1-5. Top left shows the source 51 of the raw material from which it is fed to the supply tank 52; in addition, the image shows a mill 53 designed for suitable grinding of the raw material, and a pump 54 for feeding the material into the reactor. The pump 54 also sucks in the required amount of enzyme from the container 55 for the enzyme, in which the enzyme can be suitably diluted. Components 52-55 do not form part of the reactor according to the present invention and may include any suitable tanks, mills or pumps. In addition to the material flows in FIG. 6 also shows the circulation of inert gas from the container 13, through various reaction chambers and back to the container 13 through the manifold 11 and the compressor 12. Also shown is the container 56 for the finished processed material.

FIG. 5 also shows schematically the flow (g) of the inert gas from the container 13 through the reactor and back to the container 13 through the collector 11, possibly through a not shown return line 14 and the compressor 12.

FIG. 6 is a schematic and simplified top view of the reactor shown in FIG. 1, having a reaction chamber R1, spirally arranged around the heat exchanger HEX2, valve V1 (and valves V2, V3 located below, etc.). A pipeline 18 for feeding the raw material is also shown, but the flow of inert gas supplied to the system is not shown.

FIG. 7 is a view of an alternative embodiment shown in FIG. 1 having direct reaction chambers R1'-R4 '. When considering FIG. 8 it is not obvious that in this case the reaction chambers are also located obliquely. Additional reaction chambers can be placed below the reaction chambers: for example, the reaction chamber R5 'below the reaction chamber R1', the reaction chamber R6 'below the reaction chamber R2', etc.

FIG. 8 shows an alternative embodiment of the installation shown in the previous figures.

Shown in FIG. 8, the details have numerical designations similar to those indicated in FIG. 1, but with the addition of 100 units.

There are two main differences between the considered embodiments: one of them is that the reaction chambers R101-R107 and the pasteurization chambers P101-P103 have not a tubular shape, but the shape of more frequently used tanks, preferably without sharp corners, in which material can collect, which is undesirable. Another difference is that the reactor system is designed in such a way that it takes up less space in height, but a larger area, in particular, due to the fact that the heat exchangers HEX101 and HEX102 are located next to each other, rather than one above another, and pasteurization chambers are not located below the reaction chambers, but to the side of the reaction chambers.

Thus, the specific conditions of the location are an important factor in the choice of the most preferred embodiment; If the floor area for placement is more accessible than the height, then the option represented in FIG. 8. In addition, the system shown also includes a first heat exchanger HEX101, designed to heat the feed material to a temperature favorable for the flow of enzymatic hydrolysis, as well as a heat exchanger HEX102, designed to heat the feed mixture of materials to a higher temperature than the temperature favorable for the flow of enzymatic hydrolysis.

In addition, the presented embodiment includes seven reaction chambers R101-R107, which are mixed using an inert gas supply, and a gradual (five stages) movement of material from the reaction chamber R101 to the R107 chamber occurs, starting from the upper vertical levels, i.e. the action of gravity.

Unloading from the system can be performed by the method described above, under the action of gas supplied at elevated pressure.

Presented in FIG. 8, the system further includes three pasteurization tanks, which may have the same regular shape as the reaction chambers R101-R107. In contrast to the embodiment shown in FIG. 1, in this embodiment, it is less important that the pasteurization chambers have the same shape and size as the reaction chambers, but the choice of chambers of essentially the same shape seems natural, in particular, since the manufacture of chambers of the same size and shape is less complicated and more effective.

FIG. 8 shows the raw material feed 101, removing the processed material 102, the pipeline 118 for transporting material from the first heat exchanger to the first reaction chamber, the pipeline 117 for transporting from the last reaction chamber to the second heat exchanger, pipeline 116 leading from the second heat exchanger to the first pasteurization chamber that supplies inert gas conduit 110 and manifold 111 for reused inert gas reuse.

It should be noted that, despite the fact that in FIG. 8, details such as an inert gas compressor, a pressurized inert gas tank or supply and removal of heat carrier from heat exchangers are not shown, it will not be difficult for a technician to choose suitable equipment having these functions.

Below is a practical example of how to use a reactor in a typical situation.

Additional preferred parts

The separation wall can separate the coils 33 and 34 from the water mass in the center of each of the heat exchangers HEX1 and HEX2. This further enhances the heat exchange in countercurrent mode.

Between the coils of the coil, between the coils and the outer wall and between the coils and the dividing wall, if any, should be a "gap". This is necessary to achieve the best heat transfer. With a diameter of, for example, 60 mm, the gap may be, for example, 20 mm. If there is a separation wall, it naturally must end at an appropriate distance from the upper and lower surfaces of the heat exchangers so that the water flow can be recycled from top to bottom and bottom to top.

The heat supplied to the heat exchange units 31 and 32 is usually provided by hot water, water vapor, or a combination thereof.

In practice, the temperature of the product is mainly determined by the following factors:

a) The flow rate of the product through the coil. The speed changes over time with equal transitions (English even transitions), regulated by a pump, which can usually be a double-acting piston pump.

b) The speed of the hot water moving in counterflow to the coil can be adjusted according to the flow of the product by controlling the speed of the air supplied to the collector 35.

c) Hot water temperature. The opening of the steam / hot water entry valve to the heat exchanging device 31 can be adjusted according to the temperature of the residual raw material measured at the outlet of the heat exchanger HEX1.

The heat exchanger HEX2 is used to pasteurize the product after hydrolysis to “destroy” the enzyme activity and prevent the growth of bacteria.

During the time required for the hydrolysis of the raw material, the temperature of the raw material may decrease by approximately 3 ° C. The material is then heated in a heat exchanger HEX2, for example, to 95 ° C. The ratio between the heights of the lower (HEX1) and upper (HEX2) heat exchangers can be correlated with the temperature difference: 5-48 ° C and 45-95 ° C. After the air is bubbled through the water in both chambers, it is released into the atmosphere.

The dimensions of the reaction chambers R1-R6 can be different, but the typical diameter can be 600 mm, regardless of whether the reaction chambers are spiral-shaped or straight. The gaps between the individual chambers in which the valves are installed can be about 150 mm. Preferably, all valves present in the reactor, both for the raw material and for inert gas, etc., can be automatically controlled. The valve control method does not relate to the present invention and, therefore, is not discussed in more detail here.

The processing time in each chamber can be different and can usually be from 5 to 15 minutes. Of course, the processing time is influenced by the number of chambers in the reactor, as well as the type of raw material used.

The reactor according to the present invention is suitable for use on board fishing vessels, and in order for it to function, it does not have to be installed vertically. The slope of the reaction chambers of 1:10 (vertical / horizontal size) is usually sufficient even for work at sea. If it is necessary for the reactor to function with greater roll, the slope can be increased, for example, to 1: 5.

Although it is not the cornerstone of the present invention, it should be noted that in the embodiment of the reactor shown in FIG. 1, with the appropriate dimensions of the reaction chamber and the heat exchanger, that is, when the total height of the reactor is approximately 6 meters, the reactor can be enclosed in a standard 20-foot (20 feet approximately 6 meters) container installed vertically. The reactor shown in FIG. 8, can be designed so that it has a significantly lower overall height, but it still does not allow to enclose it in a container.

However, the principles of operation of the reactor according to the invention can be implemented regardless of whether or not such a height can be achieved. For example, the reaction chambers can be placed in the form of a column, while the pasteurization chambers can be placed in the form of a separate column installed side by side; in this case, the reactor has a smaller height and a greater width than the reactor represented in graphic materials.

In the appended claims, the symbols refer to the embodiment shown in FIG. 1-5, with the exception of PP. 14-18, which refer to FIG. 8, and p. 20, which relates to FIG. 1 and FIG. eight.

Claims (26)

1. A reactor for enzymatic hydrolysis of a material, sequentially including: - the first heat exchanger designed to heat the raw material fed into the reactor to a temperature whose value is in the range that facilitates the flow of enzymatic hydrolysis; - series-connected reaction chambers separated by closing valves; - the second heat exchanger, designed to heat the reaction mixture coming from the last reaction chamber, to a temperature in excess of the temperature range, contributing to the flow of enzymatic hydrolysis; characterized in that the design of the reactor includes reaction chambers placed at different vertical levels, where the first reaction chamber is the topmost one and the last reaction chamber is the lowest, at least one of the reaction chambers is made to mix its contents through the inert chamber gas. 2. The reactor under item 1, in which all the reaction chambers have the same size and shape and are located symmetrically relative to the vertical axis. 3. The reactor according to claim 1, wherein said reaction chambers have a tubular shape, are arranged obliquely and are connected in such a way that the assembled structure is symmetrical about the vertical axis. 4. The reactor according to any one of the preceding paragraphs, in which all the reaction chambers are made for mixing their contents by passing an inert gas through the chamber, which is supplied near the end of the reaction chambers, which is located downstream, and is discharged near that end of the reaction chambers, which is located above downstream. 5. The reactor according to any one of the preceding paragraphs, in which the reaction chambers are bent and assembled in the form of a spiral. 6. The reactor according to any one of paragraphs. 3-5, in which at least one of the first heat exchanger and the second heat exchanger is installed along the vertical axis of the reactor. 7. The reactor according to any one of paragraphs. 3-6, in which the first heat exchanger and the second heat exchanger are installed one above the other along the vertical axis of the reactor. 8. The reactor under item 6 or 7, in which the first heat exchanger and the second heat exchanger are installed one above the other, concentrically with respect to the helix, which form the reaction chambers. 9. The reactor according to any one of the preceding paragraphs, further comprising at least one pasteurization chamber located downstream of the second heat exchanger. 10. The reactor according to claim 9, in which at least one pasteurization chamber is made in the form of a tubular chamber, having essentially the same shape as the reaction chamber. 11. The reactor according to any one of paragraphs. 3 or 5-8, further comprising an outer casing in which the reaction chambers and both heat exchangers are enclosed. 12. The reactor according to any one of the preceding paragraphs, in which the inert gas is suitable for recycling and reuse. 13. The reactor according to any one of paragraphs. 3, 5-8 or 11 in which the reaction chambers have a slope with a vertical / horizontal ratio of at least 1/10. 14. The reactor according to any one of paragraphs. 1, 2, 4, 9 or 12, in which each reaction chamber is a container that has a simple, regular shape, the reaction chambers are located one above the other vertically so that the first reaction chamber is the topmost one, and the last reaction chamber is itself bottom. 15. The reactor according to claim 14, in which each reaction chamber has the lowest point located at the point of release of material from the reaction chamber. 16. The reactor according to claim 14 or 15, wherein each pasteurization chamber is a regular-shaped container, the pasteurization chambers are located one above the other vertically so that the first pasteurization chamber is the top one and the last pasteurization chamber is the bottom one. 17. The reactor according to any one of paragraphs. 14 or 15, in which the first heat exchanger is connected upstream of the reaction chamber and the second heat exchanger is connected downstream of the last reaction chamber and upstream of the first pasteurization chamber. 18. The reactor according to any one of paragraphs. 14-16, in which the reactor is composed of four groups of elements that are placed independently of each other, preferably side by side, where the first heat exchanger forms the first group, the reaction chambers form the second group, the second heat exchanger forms the third group, and the pasteurization chambers form the fourth group . 19. The reactor according to any one of the preceding paragraphs, in which each reaction chamber is made for periodic unloading by supplying to each reaction chamber an inert gas having an overpressure, and opening a downstream valve to be closed. 20. The reactor according to any one of the preceding paragraphs, wherein said first heat exchanger is designed to heat a mixture of materials to a temperature of about 50 ° C, and the second heat exchanger is to heat a mixture of materials to a temperature of at least about 90 ° C. 21. The reactor according to any one of the preceding paragraphs, comprising a feeding device or made for connection with a feeding device intended for dispensing a certain, regulated amount of enzyme and a certain amount of raw material for hydrolysis. 22. The reactor according to any one of the preceding paragraphs, where the reactor is made for mixing by passing nitrogen used as inert gas.

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