WO2008004183A2 - Plant and method for hydrolyzing a reaction mixture hydrolyzable raw material - Google Patents
Plant and method for hydrolyzing a reaction mixture hydrolyzable raw material Download PDFInfo
- Publication number
- WO2008004183A2 WO2008004183A2 PCT/IB2007/052584 IB2007052584W WO2008004183A2 WO 2008004183 A2 WO2008004183 A2 WO 2008004183A2 IB 2007052584 W IB2007052584 W IB 2007052584W WO 2008004183 A2 WO2008004183 A2 WO 2008004183A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reaction mixture
- plant
- reactor
- separation section
- completely hydrolysed
- Prior art date
Links
Classifications
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
- A23J3/00—Working-up of proteins for foodstuffs
- A23J3/30—Working-up of proteins for foodstuffs by hydrolysis
Definitions
- the invention relates to a plant for hydrolysing a reaction mixture comprising a batch of an at least partly hydrolysable, animal, marine or vegetable components or a mixture of these components, the plant is of the kind that comprises at least one reactor formed with a feed end for feeding the reaction mixture and at least one bottom discharge for discharging the completely hydrolysed reaction mixture, at least one separation section connected to the reactor via a first pipe conduit for separation of the completely hydrolysed reaction mixture into a number of fractions after discontinuation of the hydrolysis, and at least one storage container for at least one of the fractions connected to the separation section via at least one second pipe conduit.
- Such reactors are known from the inventor's own international patent applications nos . WO 2005/058059 and WO 2005/058060 for industrially producing proteinaceous , hydrolysed reaction mixtures of by-products from the food processing industry.
- the hydrolysed reaction mixture is processed further and utilized for production of e.g. soup concentrates, protein supplements, amino acids, fats, oils, lipids, and fatty acids.
- the reaction mixture is hydrolysed with its content of fat and protein for example at a temperature of about 55°C for about one hour.
- the hydrolysis reaction can for example take place enzymatically as a result of a change in pH or be a combination of both.
- the hydrolysis reaction is stopped by increasing the temperature to about 90 - 100°C for 30 - 60 minutes, whereby any residual enzyme, whether it is added or is a natural part of the raw material of the reaction mixture, is effectively inactivated.
- the hydrolysis conditions can easily be controlled.
- the closed and well-defined batch environment is well-arranged and has uniform process conditions. Therefore, a uniform high product quality can easily be maintained.
- the batch process in these known plants takes relatively long as the reactor itself is used both as reactor, holding tank, and separation tank, and these known batch processes are therefore only preferred for smaller productions for economic and operational reasons.
- a semi- continuous plant for hydrolysing a fat and/or proteinaceous mixture of raw material that has a high efficiency and high productivity.
- a semi- continuous method for hydrolysing large amounts of fat and/or proteinaceous mixture of raw material faster than hitherto known.
- the novel and unique feature according to the invention is the fact that the plant comprises a tank inserted in the first pipe conduit for completely hydrolysed reaction mixture and one or more reactors connected to the tank simultaneously or in turns. By connecting one or more of the reactors to the tank in turns, the capacity of each reactor can be exploited optimally.
- the first portion of completely hydrolysed reaction mixture is discharged into the tank for storage with the object of further processing in the separation section.
- the hydrolysis of a second, third, and next batch in a second, third, and next reactor has already begun, and these batches are continuously discharged into the tank as they become completely hydrolysed.
- the tank can for example be dimensioned to a maximum size corresponding to the volume of all the reactors inserted in the first pipe conduit at one time but is typically smaller as the tank is emptied continuously to the separation section while new batches of completely hydrolysed reaction mixture are produced in the reactors .
- the tank can advantageously be provided with means, for example a screw conveyor, for quickly conveying the continuously supplied completely hydrolysed reaction mixture in a direction towards the separation section. If the screw conveyor is rotated, the completely hydrolysed reaction mixture with its mixed content of insoluble and soluble components, for example bone fragments, meat, coagula, dissolved protein, peptides, amino acids, fat and fatty acids, respectively, is conveyed in a simple manner to the separation section.
- the separation section can be a vibrating screen. Suited vibrating screens can for example be the vibrating screen described in European patent application No. EP 0699 109, or a Russell Finex Separator produced by Russell Finex Ltd. , Feltham, Middlesex, Great Britain.
- the hydrolysed reaction mixture can be divided into fractions in a simple manner, said fractions are passed further on to separate collection containers in closed pipe conduits via the at least one second pipe conduit, for example a number of collection containers corresponding to the number of fractions produced at any one time in the separation section.
- the completely hydrolysed reaction mixture can e.g. be divided into three fractions, each passed on to a first collection container for bone from the reaction mixture, a second collection container for insoluble components smaller than bone, and a third collection container for soluble components and fat .
- the separation section can e.g. merely be a separating tank, in which the completely hydrolysed reaction mixture remains until the heavy, insoluble components in the hydrolysed reaction mixture have settled on the bottom of the tank, overlaid by lighter components and fluid according to the same principles as described in the inventor's own international patent applications WO 2005/058059 and WO 2005/058060.
- a fat phase can appear very early in the hydrolysis reaction on top of the reaction mixture in every reactor.
- This fat phase can advantageously be discharged via an upper outlet located nearest to a feeding end of each reactor, said outlet being connected either directly to the separation section via a third pipe conduit in case this fat phase contains floating components, such as e.g. chicken skin, or to the third collection container if the fat phase is not fouled by larger components.
- the invention also relates to a method for hydrolysis of a reaction mixture comprising a batch of at least partly hydrolysable animal, marine, or vegetable components or a mixture of these components, in which the method in a first step comprises heating the reaction mixture to a hydrolysis temperature in at least one reactor, in a second step maintaining the reaction mixture in the at least one reactor for a specified hydrolysis time, in a third step stopping the hydrolysis reaction to obtain a batch of completely hydrolysed reaction mixture, and in a fourth step passing a batch of completely hydrolysed reaction mixture on to the tank.
- the fractions produced in the separation section are collected in separate collection containers for later processing and/or use.
- Tank and separation section are chosen on the basis of the number of reactors, and within the scope of the present invention, the plant can be enlarged to comprise several separation sections, collection containers, and possible several tanks which can be inserted in turns or simultaneously in the relevant pipe conduit in the plant.
- At least one of the steps may comprise prior and/or supplemental supply of inert gas or mixture of inert gasses, preferably nitrogen.
- inert gas or mixture of inert gasses preferably nitrogen.
- Mixtures of inert gases, that is gasses that do not react with the plant or the reaction mixture, are also comprised within the scope of the present invention.
- a possible fat phase which in some cases gradually can accumulate at the top of the reaction mixture in the reactor during the hydrolysis, can be passed on to a fat collection container in a simple manner before the completely hydrolysed reaction mixture is passed on to the separation section.
- An exemplary reaction mixture that can be hydrolysed in the plant according to the invention can merely comprise water and meaty bones from e.g. abattoirs but can also comprise many other by-products from the food processing industry, such as different raw material compositions of another origin, that is not necessarily by-products from the food processing industry.
- the reaction mixture can also comprise proteolytic and/or lipolytical enzymes for increasing the reaction rate in the reactor.
- the exemplary plant shown in fig. 1 is designated generally by the reference numeral 1.
- the plant 1 comprises five identical reactors 2, of which only one reactor is given a reference numeral for clarity.
- the reactor 2 is connected to a tank 4 via a first pipe conduit 3.
- the tank 4 is provided with a screw conveyor 5 continuously conveying completely hydrolysed reaction mixture to separation section in form of a vibrating screen 6.
- the vibrating screen 6 has an upper outlet 7 which, via a second pipe conduit 8, is connected to a first collection container 9 for coarse components, a centre outlet 10 which, via a second pipe conduit 11 is connected to a second collection container 12 for less coarse components, and a bottom outlet 13 which, via a second pipe conduit 14, is connected to a third collection container 15 for fluid and particulate components.
- the reactor 2 has a feed end 16 for feeding the raw materials that are components in the reaction mixture and at least one bottom discharge 17 for discharging the inactivated, completely hydrolysed reaction mixture in batches via a valve 18.
- a stirring device 19 driven by a motor 20 is mounted in the reactor 2.
- the reactor 2 is enclosed in a heating jacket 21, by means of which the temperature in the reactor can be adjusted partly to maintain a reaction temperature and partly to increase the temperature to inactivate the enzyme activity in the reaction mixture and discontinue the hydrolysis.
- the vibrating screen 6 has two screens 22,23.
- the screen 22 is located immediately under the outlet 7 for the second conduit pipe 8 for coarse components and serves for separating the largest and coarsest components, such as bones from the completely hydrolysed reaction mixture as a separate first fraction.
- the screen 22 has a coarser mesh width than the screen 23 which is located under the screen 22 immediately under the outlet 10 for the second pipe conduit 11 for less coarse components but above the outlet 13 for the second pipe conduit 14 for fluid and particulate components so that medium-sized components can be separated via the second pipe conduit 11 as a separate second fraction.
- the third fraction which is collected in the third collection container 15 contains i.a. fat, soluble protein and any decomposition products from such compounds .
- the screens 22,23 are preferably chosen with a mesh width that completely removes the visible components from the third fraction but within the scope of the present invention, the third fraction can instead be clarified further in a subsequent step, for example in a centrifuge if this is considered necessary. Bone fragments from the boiled bone processed in the reactor are typically removed in the first fraction.
- a larger mesh width can for example be chosen if it contributes to increasing the production speed so that the vibrating screen 6 does not represent a bottleneck in the plant.
- the principles of the mode of operations of the vibrating screen will be known to a person skilled in the art and several vibrating screens can be inserted in the plant.
- a possible fat phase can be passed via an outlet 25 at the feed end 16 of the reactor 2 on to the third collection container 13 or alternatively to a separate fat phase collection container or passed on to the vibrating screen 6.
- the tank 4 is inserted in the first pipe conduit 3 under the bottom outlet 17 of five mainly vertically mounted, identical reactors 2 so that the completely hydrolysed reaction mixture in each reactor can be drained directly down into the tank 4 simultaneously or one or more in turns, after which the emptied reactor quickly can be made ready for operation again.
- the tank 22 narrows and inclines in a direction towards the top inlet 26 to the vibrating screen 6 in a direction away from the bottom of the tank 4 in such a way that the solid components, especially the bones, will be washed by the fluid part of the completely hydrolysed reaction mixture in the tank when the completely hydrolysed reaction mixture by means of the screw conveyor 5 driven by a motor 26 is conveyed to the vibrating screen 6.
- the hydrolysis in one reactor is carried out as an independent batch process independent of the hydrolysis in another reactor which is carried out as a second and independent batch process. Therefore if a batch is damaged, the extent of the damage is limited to the reactor content in one reactor. This reactor can be emptied without the plant having to be shut completely down as the remaining reactors still can be exploited.
- the controlled reaction conditions of the batch process and safe process conditions are combined with the fast processing of the reaction mixture of this continuous process .
- the number of reactors is not limited to five within the scope of the present invention, and more or fewer reactors can be implemented in the plant depending on the size of the other parts of the plant.
- the screw conveyor can alternatively be a conveyor belt, and the separation section can e.g. be a tricanter.
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Nutrition Science (AREA)
- Biochemistry (AREA)
- Engineering & Computer Science (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A plant (1) for hydrolysing a reaction mixture comprising a batch of at least partly hydrolysable animal, marine, or vegetable components or a mixture of these components, the plant (1) is of the kind that comprises at least one reactor (2) formed with a feed end (16) for feeding the reaction mixture and at least one bottom outlet (17) for discharging the completely hydrolysed reaction mixture, at least one separation section (6) connected to the reactor (2) via a first pipe conduit (3) for dividing the completely hydrolysed reaction mixture into a number of fractions after discontinuation of the hydrolysis, and at least one storage container (9; 12; 15) connected to the separation section (6) via at least one second pipe conduit (8; 11;14) for at least one of the fractions. The plant (1) comprises a tank (4) inserted in the first pipe conduit (3) for completely hydrolysed reaction mixture and one or more reactors (2) connected to the tank (4) simultaneously or in turns. The plant has a fast processing time and a large capacity.
Description
Plant and method for hydrolysing a reaction mixture of hydrolysable raw material
The invention relates to a plant for hydrolysing a reaction mixture comprising a batch of an at least partly hydrolysable, animal, marine or vegetable components or a mixture of these components, the plant is of the kind that comprises at least one reactor formed with a feed end for feeding the reaction mixture and at least one bottom discharge for discharging the completely hydrolysed reaction mixture, at least one separation section connected to the reactor via a first pipe conduit for separation of the completely hydrolysed reaction mixture into a number of fractions after discontinuation of the hydrolysis, and at least one storage container for at least one of the fractions connected to the separation section via at least one second pipe conduit.
Such reactors are known from the inventor's own international patent applications nos . WO 2005/058059 and WO 2005/058060 for industrially producing proteinaceous , hydrolysed reaction mixtures of by-products from the food processing industry. The hydrolysed reaction mixture is processed further and utilized for production of e.g. soup concentrates, protein supplements, amino acids, fats, oils, lipids, and fatty acids.
In these known reactors, the reaction mixture is hydrolysed with its content of fat and protein for example at a temperature of about 55°C for about one hour. The hydrolysis reaction can for example take place enzymatically as a result of a change in pH or be a combination of both. The hydrolysis reaction is stopped by increasing the temperature to about 90 - 100°C for 30 - 60 minutes, whereby any residual enzyme, whether it is added or is a natural part of the raw material of the reaction mixture, is effectively inactivated.
In a batch process, the hydrolysis conditions can easily be controlled. The closed and well-defined batch environment is well-arranged and has uniform process conditions. Therefore, a uniform high product quality can easily be maintained. However, the batch process in these known plants takes relatively long as the reactor itself is used both as reactor, holding tank, and separation tank, and these known batch processes are therefore only preferred for smaller productions for economic and operational reasons.
In plants for continuous hydrolysis, it is very difficult to ensure uniform hydrolysis conditions for the entire reaction mixture and to keep a constant, uniform product quality. The entire plant has to be stopped in case the plant blocks up, or if a failure occurs in any way in the reactor. Such unintended discontinuations or prolongations of the process are very costly as the entire content in the plant most often must be discarded, the plant renovated and/or the failure remedied before resumption of operation.
In a first aspect according to the present invention, a semi- continuous plant for hydrolysing a fat and/or proteinaceous mixture of raw material is provided that has a high efficiency and high productivity.
In a second aspect according to the present invention, a semi- continuous method is provided for hydrolysing large amounts of fat and/or proteinaceous mixture of raw material faster than hitherto known.
The novel and unique feature according to the invention, whereby this is achieved, is the fact that the plant comprises a tank inserted in the first pipe conduit for completely hydrolysed reaction mixture and one or more reactors connected to the tank simultaneously or in turns.
By connecting one or more of the reactors to the tank in turns, the capacity of each reactor can be exploited optimally. As soon as a first batch has been completely hydrolysed in a first reactor, the first portion of completely hydrolysed reaction mixture is discharged into the tank for storage with the object of further processing in the separation section. At the same time, the hydrolysis of a second, third, and next batch in a second, third, and next reactor has already begun, and these batches are continuously discharged into the tank as they become completely hydrolysed. As soon as one reactor has been emptied, it can be examined, cleaned and started again with a fresh reaction mixture. That is to say that at least one reactor inserted in the first pipe conduit will always be in operation in the plant according to the present invention, and several will typically be in operation at a time. Such a plant is fast and efficient in operation and can process very large amounts of reaction mixtures without shutdowns.
The tank can for example be dimensioned to a maximum size corresponding to the volume of all the reactors inserted in the first pipe conduit at one time but is typically smaller as the tank is emptied continuously to the separation section while new batches of completely hydrolysed reaction mixture are produced in the reactors .
The tank can advantageously be provided with means, for example a screw conveyor, for quickly conveying the continuously supplied completely hydrolysed reaction mixture in a direction towards the separation section. If the screw conveyor is rotated, the completely hydrolysed reaction mixture with its mixed content of insoluble and soluble components, for example bone fragments, meat, coagula, dissolved protein, peptides, amino acids, fat and fatty acids, respectively, is conveyed in a simple manner to the separation section.
In a preferred embodiment of the plant according to the present invention, the separation section can be a vibrating screen. Suited vibrating screens can for example be the vibrating screen described in European patent application No. EP 0699 109, or a Russell Finex Separator produced by Russell Finex Ltd. , Feltham, Middlesex, Great Britain.
By means of a vibrating screen, the hydrolysed reaction mixture can be divided into fractions in a simple manner, said fractions are passed further on to separate collection containers in closed pipe conduits via the at least one second pipe conduit, for example a number of collection containers corresponding to the number of fractions produced at any one time in the separation section.
The completely hydrolysed reaction mixture can e.g. be divided into three fractions, each passed on to a first collection container for bone from the reaction mixture, a second collection container for insoluble components smaller than bone, and a third collection container for soluble components and fat .
Within the scope of the present invention, other types of apparatuses for separating the completely hydrolysed reaction mixture into fractions can just as well be used. The separation section can e.g. merely be a separating tank, in which the completely hydrolysed reaction mixture remains until the heavy, insoluble components in the hydrolysed reaction mixture have settled on the bottom of the tank, overlaid by lighter components and fluid according to the same principles as described in the inventor's own international patent applications WO 2005/058059 and WO 2005/058060.
On hydrolysis of some compositions of especially fatty reaction mixtures, a fat phase can appear very early in the hydrolysis reaction on top of the reaction mixture in every
reactor. This fat phase can advantageously be discharged via an upper outlet located nearest to a feeding end of each reactor, said outlet being connected either directly to the separation section via a third pipe conduit in case this fat phase contains floating components, such as e.g. chicken skin, or to the third collection container if the fat phase is not fouled by larger components.
The invention also relates to a method for hydrolysis of a reaction mixture comprising a batch of at least partly hydrolysable animal, marine, or vegetable components or a mixture of these components, in which the method in a first step comprises heating the reaction mixture to a hydrolysis temperature in at least one reactor, in a second step maintaining the reaction mixture in the at least one reactor for a specified hydrolysis time, in a third step stopping the hydrolysis reaction to obtain a batch of completely hydrolysed reaction mixture, and in a fourth step passing a batch of completely hydrolysed reaction mixture on to the tank.
These method steps are repeated continuously in a plant according to the invention at the same time as the completely hydrolysed reaction mixture continuously is passed from the tank to the separation section in a fifth step, the completely hydrolysed reaction mixture continuously being divided in the separation section into separate fractions in a sixth step.
Advantageously, the fractions produced in the separation section are collected in separate collection containers for later processing and/or use.
The reactor capacity of the plant can thus be exploited in optimum manner, and very large amounts of raw material can be processed without interruption of operation. Tank and separation section are chosen on the basis of the number of reactors, and within the scope of the present invention, the
plant can be enlarged to comprise several separation sections, collection containers, and possible several tanks which can be inserted in turns or simultaneously in the relevant pipe conduit in the plant.
To prevent rancidification of fatty substances in the reaction mixture, at least one of the steps may comprise prior and/or supplemental supply of inert gas or mixture of inert gasses, preferably nitrogen. Mixtures of inert gases, that is gasses that do not react with the plant or the reaction mixture, are also comprised within the scope of the present invention.
A possible fat phase, which in some cases gradually can accumulate at the top of the reaction mixture in the reactor during the hydrolysis, can be passed on to a fat collection container in a simple manner before the completely hydrolysed reaction mixture is passed on to the separation section.
The invention will be described in greater details with reference to the only figure in the drawing, which purely is an exemplary schematic diagram of a plant according to the present invention having five reactors.
An exemplary reaction mixture that can be hydrolysed in the plant according to the invention can merely comprise water and meaty bones from e.g. abattoirs but can also comprise many other by-products from the food processing industry, such as different raw material compositions of another origin, that is not necessarily by-products from the food processing industry.
The reaction mixture can also comprise proteolytic and/or lipolytical enzymes for increasing the reaction rate in the reactor.
The exemplary plant shown in fig. 1 is designated generally by the reference numeral 1.
The plant 1 comprises five identical reactors 2, of which only one reactor is given a reference numeral for clarity.
The reactor 2 is connected to a tank 4 via a first pipe conduit 3. The tank 4 is provided with a screw conveyor 5 continuously conveying completely hydrolysed reaction mixture to separation section in form of a vibrating screen 6. The vibrating screen 6 has an upper outlet 7 which, via a second pipe conduit 8, is connected to a first collection container 9 for coarse components, a centre outlet 10 which, via a second pipe conduit 11 is connected to a second collection container 12 for less coarse components, and a bottom outlet 13 which, via a second pipe conduit 14, is connected to a third collection container 15 for fluid and particulate components.
The reactor 2 has a feed end 16 for feeding the raw materials that are components in the reaction mixture and at least one bottom discharge 17 for discharging the inactivated, completely hydrolysed reaction mixture in batches via a valve 18. A stirring device 19 driven by a motor 20 is mounted in the reactor 2. The reactor 2 is enclosed in a heating jacket 21, by means of which the temperature in the reactor can be adjusted partly to maintain a reaction temperature and partly to increase the temperature to inactivate the enzyme activity in the reaction mixture and discontinue the hydrolysis.
The vibrating screen 6 has two screens 22,23. The screen 22 is located immediately under the outlet 7 for the second conduit pipe 8 for coarse components and serves for separating the largest and coarsest components, such as bones from the completely hydrolysed reaction mixture as a separate first fraction. The screen 22 has a coarser mesh width than the screen 23 which is located under the screen 22 immediately under the outlet 10 for the second pipe conduit 11 for less coarse components but above the outlet 13 for the second pipe conduit 14 for fluid and particulate components so that
medium-sized components can be separated via the second pipe conduit 11 as a separate second fraction. The third fraction which is collected in the third collection container 15 contains i.a. fat, soluble protein and any decomposition products from such compounds .
The screens 22,23 are preferably chosen with a mesh width that completely removes the visible components from the third fraction but within the scope of the present invention, the third fraction can instead be clarified further in a subsequent step, for example in a centrifuge if this is considered necessary. Bone fragments from the boiled bone processed in the reactor are typically removed in the first fraction.
A larger mesh width can for example be chosen if it contributes to increasing the production speed so that the vibrating screen 6 does not represent a bottleneck in the plant. The principles of the mode of operations of the vibrating screen will be known to a person skilled in the art and several vibrating screens can be inserted in the plant.
Via a third pipe conduit 24, a possible fat phase can be passed via an outlet 25 at the feed end 16 of the reactor 2 on to the third collection container 13 or alternatively to a separate fat phase collection container or passed on to the vibrating screen 6.
The tank 4 is inserted in the first pipe conduit 3 under the bottom outlet 17 of five mainly vertically mounted, identical reactors 2 so that the completely hydrolysed reaction mixture in each reactor can be drained directly down into the tank 4 simultaneously or one or more in turns, after which the emptied reactor quickly can be made ready for operation again. The tank 22 narrows and inclines in a direction towards the top inlet 26 to the vibrating screen 6 in a direction away
from the bottom of the tank 4 in such a way that the solid components, especially the bones, will be washed by the fluid part of the completely hydrolysed reaction mixture in the tank when the completely hydrolysed reaction mixture by means of the screw conveyor 5 driven by a motor 26 is conveyed to the vibrating screen 6.
The hydrolysis in one reactor is carried out as an independent batch process independent of the hydrolysis in another reactor which is carried out as a second and independent batch process. Therefore if a batch is damaged, the extent of the damage is limited to the reactor content in one reactor. This reactor can be emptied without the plant having to be shut completely down as the remaining reactors still can be exploited.
In the plant according to the invention, the controlled reaction conditions of the batch process and safe process conditions are combined with the fast processing of the reaction mixture of this continuous process .
The number of reactors is not limited to five within the scope of the present invention, and more or fewer reactors can be implemented in the plant depending on the size of the other parts of the plant. The screw conveyor can alternatively be a conveyor belt, and the separation section can e.g. be a tricanter.
Claims
1. A plant (1) for hydrolysing a reaction mixture comprising a batch of at least partly hydrolysable animal, marine, or vegetable components or a mixture of these components, the plant (1) is of the kind that comprises at least one reactor (2) formed with a feed end (16) for feeding the reaction mixture and at least one bottom outlet (17) for discharging the completely hydrolysed reaction mixture, at least one separation section (6) connected to the reactor (2) via a first pipe conduit (3) for dividing the completely hydrolysed reaction mixture into a number of fractions after discontinuation of the hydrolysis, and at least one storage container (9,-12,-15) connected to the separation section (6) via at least one second pipe conduit (8; 11; 14) for at least one of the fractions, characterised in that the plant (1) comprises a tank (4) inserted in the first pipe conduit (3) for completely hydrolysed reaction mixture and one or more reactors (2) connected to the tank (4) simultaneously or in turns.
2. A plant (1) according to claim 2, characterised in that the tank (4) comprises means for conveying the completely hydrolysed reaction mixture in a direction towards the separation section (6) .
3. A plant (1) according to claim 3, characterised in that the means for conveying the completely hydrolysed reaction mixture in a direction towards the separation section (6) is a screw conveyor (24) .
4. A plant (1) according to claim 1, 2, or 3 , characterised in that the separation section is a vibrating screen (6) .
5. A plant (1) according to any of the claims 1 - 4, characterised in that the at least one collection container (9,-12; 15) comprises a first collection container (9) for bones from the reaction mixture, a second collection container (12) for insoluble components smaller than the bones, and a third collection container (15) for soluble components and fat.
6. A plant (1) according to any of the claims 1 - 5, characterised in that one or more of the reactors (2) comprise an upper outlet (25) located nearest the feed end (16) of the reactor (2) , said outlet being connected to the third collection container (15) or the separation section (6) via a third pipe conduit (24) .
7. A method for hydrolysing a reaction mixture comprising a batch of at least partly hydrolysable animal, marine, or vegetable components or a mixture of these components, wherein the method comprises the steps of heating the reaction mixture to a hydrolysis temperature in at least one reactor (2) in a first step, maintaining the reaction mixture in the at least one reactor (1) for a specified hydrolysis time in a second step, stopping the hydrolysis reaction to obtain a batch of completely hydrolysed reaction mixture in a third step, and passing the batch of completely hydrolysed reaction mixture to the tank (4) in a fourth step, characterised in that the at least one reactor (2) is installed in the plant (1) according to any of the claims 1 - 6, steps 1 - 4 are repeated continuously at the same time as the completely hydrolysed reaction mixture is passed continuously from the tank (4) to the separation section (6) in a fifth step, in which the completely hydrolysed reaction mixture is continuously divided into separate fractions in a sixth, step.
8. A method according to claim 7 , characterised in that the method comprises collecting the fractions produced in the separation section (6) in separate collection containers (9,-12,-15) .
9. A method according to claim 7 or 8 , characterised in that at least one of the steps comprises prior and/or supplemental supply of inert gas or mixture of inert gasses .
10. A method according to claim 7, 8, or 9, characterised in that a fat phase formed at top of the reaction mixture in the at least one reactor (2) during hydrolysis is passed on to a separate fat collection container or the third collection container (15) before the completely hydrolysed reaction mixture is passed on to the separation section (6) .
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DKPA200600920 | 2006-07-04 | ||
| DK200600920A DK200600920A (en) | 2006-07-04 | 2006-07-04 | Plant and method for hydrolyzing a reaction mixture of hydrolysable feedstock |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2008004183A2 true WO2008004183A2 (en) | 2008-01-10 |
| WO2008004183A3 WO2008004183A3 (en) | 2008-04-24 |
Family
ID=38894967
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/IB2007/052584 WO2008004183A2 (en) | 2006-07-04 | 2007-07-03 | Plant and method for hydrolyzing a reaction mixture hydrolyzable raw material |
Country Status (2)
| Country | Link |
|---|---|
| DK (1) | DK200600920A (en) |
| WO (1) | WO2008004183A2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3212765B1 (en) * | 2014-10-27 | 2021-12-08 | Firmenich SA | Apparatus and method for hydrolysing a product |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2352498A1 (en) * | 1976-05-25 | 1977-12-23 | Belhomme Philippe | Prepn. of fish protein concentrate by enzyme hydrolysis of fish - followed by sepn. of sediment oil and proteolysis juice |
| WO2005058060A1 (en) * | 2003-12-18 | 2005-06-30 | Danflavour Aps | A plant for enzymatic hydrolysis of a batch of animal or vegetable components and method for using the plant |
-
2006
- 2006-07-04 DK DK200600920A patent/DK200600920A/en not_active Application Discontinuation
-
2007
- 2007-07-03 WO PCT/IB2007/052584 patent/WO2008004183A2/en active Application Filing
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2352498A1 (en) * | 1976-05-25 | 1977-12-23 | Belhomme Philippe | Prepn. of fish protein concentrate by enzyme hydrolysis of fish - followed by sepn. of sediment oil and proteolysis juice |
| WO2005058060A1 (en) * | 2003-12-18 | 2005-06-30 | Danflavour Aps | A plant for enzymatic hydrolysis of a batch of animal or vegetable components and method for using the plant |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3212765B1 (en) * | 2014-10-27 | 2021-12-08 | Firmenich SA | Apparatus and method for hydrolysing a product |
Also Published As
| Publication number | Publication date |
|---|---|
| DK200600920A (en) | 2008-01-05 |
| WO2008004183A3 (en) | 2008-04-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP1575374B2 (en) | Apparatus and method for hydrolysis of a protein containing raw material | |
| KR101336117B1 (en) | Method and system for processing of aquatic species | |
| US9464309B2 (en) | Methods for recovering peptides/amino acids and oil/fat from one or more protein-containing raw materials, and products produced by the methods | |
| JP2022051833A (en) | Improved methods and systems for recovering protein powder and natural omega-3 oil from animal tissue | |
| ZA200107966B (en) | Method for recycling pet components and device for carrying out said method. | |
| EA014093B1 (en) | Apparatus and method for separation of waste material | |
| WO2008004183A2 (en) | Plant and method for hydrolyzing a reaction mixture hydrolyzable raw material | |
| WO2012094067A1 (en) | Method and system for non destructive lean recovery | |
| JP2000061432A (en) | Organic waste treating method and device | |
| AU606091B2 (en) | A process for producing protein products from bone-containing animal material Case abandoned | |
| Prokop | Rendering systems for processing animal by-product materials | |
| RU2123789C1 (en) | Method and apparatus for complex reprocessing of slaughter house wastes | |
| US4157335A (en) | Fat recovery system | |
| WO2008004182A2 (en) | Reactor, plant and method for hydrolyzing a reaction mixture hydrolyzable raw material and a protein composition obtained thereby | |
| RU2719508C1 (en) | Albuminous cloudiness of brewer grains, method and apparatus for production thereof | |
| JP2001170937A (en) | Regeneration-processing installation for film waste and method for regeneration-processing film waste | |
| GB2612617A (en) | Demineralisation of organic tissue | |
| CN104903015B (en) | The device and method of at least one pure substance are obtained from biological waste or biomass | |
| KR20240095314A (en) | Demineralization of organic tissue | |
| RU2333663C2 (en) | Method of peptide/amino acids production from raw material containing protein, associated products and application of products | |
| RU58858U1 (en) | LINE FOR INTEGRATED PROCESSING OF HYDROBIONES AND PRODUCTION OF PROTEIN ENZYMATIC HYDROLYSES | |
| WO2001066270A1 (en) | Method and apparatus for processing eggshells | |
| CN109673712B (en) | Tooth-removing method for pleurotus nebrodensis | |
| SU1762882A1 (en) | Conveyer for manufacturing dry animal feeds | |
| WO2005058060A1 (en) | A plant for enzymatic hydrolysis of a batch of animal or vegetable components and method for using the plant |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| NENP | Non-entry into the national phase in: |
Ref country code: DE |
|
| NENP | Non-entry into the national phase in: |
Ref country code: RU |
|
| 122 | Ep: pct application non-entry in european phase |
Ref document number: 07825882 Country of ref document: EP Kind code of ref document: A2 |