CA2155042A1 - Process for the preparation of protein-rich product from brewer's spent grain - Google Patents
Process for the preparation of protein-rich product from brewer's spent grainInfo
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- CA2155042A1 CA2155042A1 CA002155042A CA2155042A CA2155042A1 CA 2155042 A1 CA2155042 A1 CA 2155042A1 CA 002155042 A CA002155042 A CA 002155042A CA 2155042 A CA2155042 A CA 2155042A CA 2155042 A1 CA2155042 A1 CA 2155042A1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
- Y02P60/80—Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
- Y02P60/87—Re-use of by-products of food processing for fodder production
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- General Preparation And Processing Of Foods (AREA)
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
Abstract
A high protein content product is obtained from BSG
containing husks and a proteinaceous material adhering to the husks, by a process including the steps of:
(a) pressing BSG in wet state to separate the proteinaceous material from the husks and to ground the proteinaceous material;
(b) dispersing the product of step (a) in water to obtain a slurry;
(c) filtering the slurry with a sieve to obtain a filtrate containing the ground proteinaceous material and a solid residue;
(d) separating the filtrate into a condensed slurry containing the ground proteinaceous material and a supernatant;
(e) separating the condensed slurry into a solid-rich phase and a liquid phase;
(f) contacting the solid-rich phase with a hot gas while maintaining the solid-rich phase such that the solid-rich phase is dried to have a water content of 15 % by weight or less within 60 seconds.
containing husks and a proteinaceous material adhering to the husks, by a process including the steps of:
(a) pressing BSG in wet state to separate the proteinaceous material from the husks and to ground the proteinaceous material;
(b) dispersing the product of step (a) in water to obtain a slurry;
(c) filtering the slurry with a sieve to obtain a filtrate containing the ground proteinaceous material and a solid residue;
(d) separating the filtrate into a condensed slurry containing the ground proteinaceous material and a supernatant;
(e) separating the condensed slurry into a solid-rich phase and a liquid phase;
(f) contacting the solid-rich phase with a hot gas while maintaining the solid-rich phase such that the solid-rich phase is dried to have a water content of 15 % by weight or less within 60 seconds.
Description
~ -- 1 --Background of the Invention This invention relates to a process for the preparation of a high protein content product from brewer's spent grain (hereinafter referred to as BSG).
BSG is a saccharification residue of brewer's malt (optionally containing rice, corn grits, corn grits, corn starch, etc.) and is obtained as a by-product in the production of beer. Usually, the BSG is separated from wort in a wet state by means of a solid-liquid separator such as a lauter tub or a mash filter, and has a water content of about 80 ~ by weight and contains about 25 ~ of proteins on dry basis.
United States patent No. 3,846,397 discloses a process of recovering proteins from BSG, in which BSG is heated in an alkaline solution. One serious problem of this process is deterioration of the quality of the product due to the heat and alkali treatments.
United States patent No. 5,1135,765 (Kish et al) discloses a process for producing a protein-rich product from BSG, in which BSG in a wet state is passed through a roll mill and is then sieved to recover a protein-rich product.
Since this process uses only physical treatments such as roll milling and sieving without resorting to a chemical treatment such as an alkali treatment, the protein-rich product is quite safe for feed and food, and has a very high protein content. In this process, the protein-rich product as sieved is dried in vacuum to produce a dried product. Since the as sieved product has a very high water content, the vacuum evaporation method is not industrially applicable for reasons of economy.
Summary of the Invention It is, therefore, the primary object of the present invention to provide an economical process which can produce a dry high protein content product from BSG on a large scale.
Another object of the present invention is to provide a process of the above-mentioned type which can produce a high quality product with a high yield.
In accomplishing the above objects, there is provided in accordance with the present invention a process for the preparation of a high protein content product from brewer's spent grain containing husks and a proteinaceous material adhering to the husks, comprising the steps of:
(a) pressing the brewer's spent grain having a water content of at least 65 % by weight to separate said proteinaceous material from said husks with simultaneous grinding of said proteinaceous material;
(b) dispersing the product obtained in step (a) in water to obtain a slurry having a solid matter content of 3-5 % by weight;
(c) filtering said slurry with a sieve having a mesh size of 30-60 mesh to obtain a filtrate containing said ground proteinaceous material and a solid residue;
(d) separating said filtrate into a condensed slurry containing 0.5-2 % by weight of said ground proteinaceous material and a supernatant;
(e) separating said condensed slurry into a solid-rich phase having a water content of 70-95 ~ by weight and a liquid phase;
(f) contacting said solid-rich phase with a hot gas while maintaining said solid-rich phase at a temperature not higher than 100C such that said solid-rich phase is dried to have a water content of 15 % by weight or less within 60 seconds, thereby obtaining said high protein content product.
Brief Description of the Drawing Other objects, features and advantages of the present invention will become apparent from the detailed description of the preferred embodiments of the invention which follows, when considered in light of the accompanying drawing, in which:
the sole FIGURE is a schematic flow diagram showing an apparatus suitable for carrying out the process according to the present invention.
_ 3 _ ~ 21 55 042 Detailed Description of the Preferred Embodiments of the Invention BSG is constituted by husks, germs and other particles having protein contents of about 5 ~ by weight, 50 % by weight and 50 % by weight, respectively. The germs and other particles are bound to or adhered to the husks. In the present specification, the germs and other particles are commonly referred to as "proteinaceous material". BSG
separated from wort and having a water content of about 70-80 % by weight may be used as such for the purpose of the present invention. The BSG concentrated or dried for easiness in storage and transportation may also be used for the purpose of the present invention after addition of water to have a water content of at least 65 ~ by weight.
Referring now to FIGURE, BSG is fed through a line 21 to a pressing zone 1, preferably a roll mill, where BSG is subjected to pressing and shearing forces so that the proteinaceous material is scraped and separated from the husks with simultaneous grinding of the proteinaceous material. When a roll mill is used, it is preferred that the gap between rolls be 0.05-2 mm, more preferably 0.1-0.3 mm.
The BSG treated in the pressing zone 1 should contain at least 65 % by weight of water, since otherwise part of the husks which have a low protein content will be also pulverized and incorporated into the final product, so that the protein concentration of the product is lowered.
The press-ground product obtained in the pressing zone 1 is then introduced through a line 22 into a mixing zone 2, where the press-ground product is dispersed in water supplied through a line 41. The dispersing operation is performed with stirring by any suitable means such as a propeller-type stirring apparatus for a period of time sufficient to form a slurry, generally for 5-30 minutes, preferably 10-20 minutes. The water is used in an amount so that the resulting slurry has a solid matter content of 3-5 by weight, preferably 4-5 % by weight.
215SOg2 The slurry is fed through a line 23 to a first sieving zone 3 and is filtered with a sieve having a mesh size of 30-60 mesh (0.213-0.567 mm) to obtain a filtrate, in the form of a slurry, containing the ground proteinaceous material and a solid residue containing the husks. The sieve used in the sieving zone 3 is preferably of a vibrating-type.
The ground proteinaceous material generally has a protein content of 50-52 % by weight on dry basis.
The filtrate is fed through a line 30 to a first separation zone 6. Preferably, the solid residue obtained in the first sieving zone 3 is fed to a second mixing zone 4, where the solid residue is dispersed in water supplied through a line 42 to obtain a mixture, in the form of a slurry, having a solid matter content of 3-5 % by weight, preferably 4-5 % by weight. As a result of this treatment, the ground proteinaceous material remaining, in a small amount, in the solid residue is separated therefrom. The mixture is fed through a line 25 to a second sieving zone 5 and is filtered with a sieve having a mesh size of 30-60 mesh (0.213-0.567 mm) to a first phase (filtrate) which has passed through the sieve and which contains a small amount of the ground proteinaceous material and a second phase (solid residue) which has remained on the sieve and which is substantially free of the ground proteinaceous material. The first phase (filtrate) obtained in the second sieving zone 5 is fed to the first separation zone 6 through a line 26 together with the filtrate from the first sieving zone 3.
In the first separation zone 6, the filtrate from the sieving zones 3 and 5 is separated into a condensed slurry containing 0.5-2 % by weight of the ground proteinaceous material and a liquid phase. In one preferred embodiment, the separation zone 6 is a sedimentation tank or settler having a discharge port at the bottom thereof. The filtrate fed to the sedimentation tank 6 is allowed to quiescently stand for 5 minutes to 2 hours, preferably 10-20 minutes, until a condensed slurry containing 0.5-2 % by weight, preferably 1-2 % by weight, of the ground 215S0~2 proteinaceous material is formed as a result of the sedimentation. During the sedimentation, the fats (vegetable oils and fats) contained in the ground proteinaceous material is dissolved into water so that the protein concentration of the ground proteinaceous material is increased. The slurry is discharged from the sedimentation tank 6 through the bottom discharge port and is introduced into a second separating zone 7 through a line 27. The supernatant obtained in the sedimentation tank 6 is fed to the water tank 13 through lines 31 and 39.
In the second separating zone 7, the slurry is separated into a solid-rich phase having a water content of 7-95 ~ by weight, preferably 80-90 ~ by weight, more preferably 80-85 ~ by weight, and a supernatant phase by any suitable dehydrating device such as a centrifuge, a drum filter, a leaf filter or a filter press. The use of a continuous centrifuge is preferred. The protein-containing solid-rich phase is fed to a drying zone 8, whereas the supernatant is fed to the water tank 13 through lines 38 and 39.
In the drying zone 8, the solid-rich phase is brought into direct contact with a hot gas to obtain a dried product. The drying should be carried out under specific conditions, since otherwise the product is discolored or deteriorated; i.e. the product becomes dark and shows a reduced digestibility by the enzyme pepsin. Thus, it is important that the solid-rich phase should be maintained at a temperature not higher than 100C, preferably 80-90C, and should be dried so that the water content of the solid-rich phase is reduced to 15 % by weight or less, preferably 10-12 ~ by weight, in a period of 60 seconds or less, preferably in a period of 30-60 seconds. The hot gas is preferably hot air and preferably has a temperature of 300-500C, more preferably 400-450C. The drying is suitably carried out with a rotary kiln-type dryer or a drum dryer.
The dried product is discharged from the drying zone through a line 29 and is recovered. The dried product ` - 6 - _ 21S5 042 generally containing lumps is preferably ground into a particle size of 0.1-1 mm and is packaged. If desired, an anti-oxidant such as ethoxyquin (for animal feeding) or Vitamin E (for food purposes).
The solid residue (husks) obtained in the sieving zone 5 is fed to a dehydrating zone 9 through a line 32. The solid residue generally has a water content of 85 % by weight or more, typically about 91 % by weight, is thus dehydrated in the zone 9 so that the dehydrated product has a water content of less than 75 ~ by weight, typically 65-70 % by weight. A screw press, a centrifuge or a filter may be used to effect the dehydration.
The dehydrated product is then fed to a combustion zone 10 through a line 33 and is combusted. The combustion zone 10 may be, for example, a fluidized bed incineration furnace or a rotary incineration furnace. The combustion waste gas is introduced through a line 34 into a heat exchanger where the heat of the combustion waste gas is recovered by indirect heat exchange with a suitable gas medium such as air. The heated medium is fed to the drying zone 8 through a line 50 as at least part of the hot gas.
The water separated in the dehydrating zone 9 is fed to a separating zone 12, preferably a sedimentation tank, through a line 35, and is allowed to quiescently stand for 5 minutes to 2 hours, preferably 10-20 minutes, so that solids contained in the water in a small amount are separated by sedimentation to form a slurry in the bottom of the sedimentation tank. The slurry, which generally contains 0.5-1.5 ~ by weight of solid matters (husks and trace amount of the proteinaceous material), is discharged through a line 36 and recycled to the dehydrating zone 9. The supernatant obtained in the sedimentation tank 12 is fed to the water tank 13 through lines 37 and 39.
The water from the separating zones 6, 7 and 12 is collected in the water tank 13 and is recycled to the mixing zones 2 and 4 through a line 40 and the lines 41 and 42.
Excess water is discharged from the tank 13 through a line ~ - 7 _ _ 21 55 0~ 2 43, while make up water is supplied to the tank 13 through a line 44.
In the above embodiment, the second mixing zone and the second sieving zone may be omitted, if desired. In this case, the solid residue separated in the sieving zone 3 is fed to the dehydrating zone 9.
The following examples will further illustrate the present invention. Parts and percentages are by weight.
Example 1 BSG (water content: 78 ~, protein content: 25.5 %
on dry basis) was treated using the system shown in the FIGURE. Thus, 100 Kg of the BSG (dry weight 22 kg) were pressed and ground with a roll mill 1 having a roll aperture of 0.1 mm.
The ground mass was then placed in a mixing tank 2 together with 447 liters of water and stirred for 10 minutes with a propeller stirrer. The resulting slurry (solid matter content: 4 ~) was filtered with a 55 mesh sieve 3 (wire net, opening: 0.250 mm) of a vibrating type to obtain 189 kg of solid residue constituted of husks (water content: 91 %, dry weight: 17 kg) as a plus fraction and 358 liters of a filtrate in the form of a slurry (solid matter content: 1.4 %, dry weight 5 kg, protein content: 52 % on dry basis) as an under-size fraction.
The solid residue was placed in a mixing tank 4 together with 236 liters of water and stirred for 10 minutes with a propeller stirrer. The resulting slurry (solid matter content: 4 ~) was filtered with a 55 mesh sieve 5 (wire net, opening: 0.250 mm) of a vibrating type to obtain as a plus fraction and 258 liters of a filtrate in the form of a slurry (solid matter content: 1 ~, dry weight 2 kg, protein content:
47 ~ on dry basis) as an under-size fraction.
The under-size fractions (total 616 liters, protein content: 50.0 ~ on dry basis) obtained by the sieving steps 3 and 5 was fed to a settler 6 and allowed to quiescently stand for lO minutes. The sediment (condensed slurry, solid matter - 8 - _ 21 55 0~2 .
content: 2 ~) was discharged from the bottom of the setter 6 and recovered. The amount of the recovered sediment was 370 liters. The supernatant (amount: 246 liters, solid matter content: 0.1 %) was also recovered.
The sediment was found to have a protein content of 52.5 ~ on dry basis. Thus, the protein content is increased by the sedimentation. The increase is considered to be ascribed to the dissolution of lipids contained in the proteinaceous material in water during the sedimentation stage.
The condensed slurry obtained in the settler 6 was dehydrated using a centrifuge 7 (3,600 G) to obtain 38 kg of protein-containing solid-rich phase (water content: 85 ~).
The solid-rich phase was fed to a rotary hot air dryer 8 and dried for 60 seconds by contact with the hot air to obtain 6 kg of protein-rich product (water content: 10 ~). The hot air had a temperature of 440C. The solid-rich phase was maintained at a temperature below 100C throughout the drying step.
The product was then ground and sieved with a 30 Tyler mesh sieve to obtain 6 kg of a pulverized product.
This was mixed with an anti-oxidant (ethoxyquin) to obtain a mixture having an ethoxyquin content of 90 ppm. The mixture was packed in plastic bags.
The solid residue (167 kg, water content: 91 %) obtained in the sieving step 5 was dehydrated with a screw press 9 to obtain 50 kg of a dehydrated product (water content: 70 ~). The dehydrated product was burned in a rotary incinerator with kerosene oil.
BSG is a saccharification residue of brewer's malt (optionally containing rice, corn grits, corn grits, corn starch, etc.) and is obtained as a by-product in the production of beer. Usually, the BSG is separated from wort in a wet state by means of a solid-liquid separator such as a lauter tub or a mash filter, and has a water content of about 80 ~ by weight and contains about 25 ~ of proteins on dry basis.
United States patent No. 3,846,397 discloses a process of recovering proteins from BSG, in which BSG is heated in an alkaline solution. One serious problem of this process is deterioration of the quality of the product due to the heat and alkali treatments.
United States patent No. 5,1135,765 (Kish et al) discloses a process for producing a protein-rich product from BSG, in which BSG in a wet state is passed through a roll mill and is then sieved to recover a protein-rich product.
Since this process uses only physical treatments such as roll milling and sieving without resorting to a chemical treatment such as an alkali treatment, the protein-rich product is quite safe for feed and food, and has a very high protein content. In this process, the protein-rich product as sieved is dried in vacuum to produce a dried product. Since the as sieved product has a very high water content, the vacuum evaporation method is not industrially applicable for reasons of economy.
Summary of the Invention It is, therefore, the primary object of the present invention to provide an economical process which can produce a dry high protein content product from BSG on a large scale.
Another object of the present invention is to provide a process of the above-mentioned type which can produce a high quality product with a high yield.
In accomplishing the above objects, there is provided in accordance with the present invention a process for the preparation of a high protein content product from brewer's spent grain containing husks and a proteinaceous material adhering to the husks, comprising the steps of:
(a) pressing the brewer's spent grain having a water content of at least 65 % by weight to separate said proteinaceous material from said husks with simultaneous grinding of said proteinaceous material;
(b) dispersing the product obtained in step (a) in water to obtain a slurry having a solid matter content of 3-5 % by weight;
(c) filtering said slurry with a sieve having a mesh size of 30-60 mesh to obtain a filtrate containing said ground proteinaceous material and a solid residue;
(d) separating said filtrate into a condensed slurry containing 0.5-2 % by weight of said ground proteinaceous material and a supernatant;
(e) separating said condensed slurry into a solid-rich phase having a water content of 70-95 ~ by weight and a liquid phase;
(f) contacting said solid-rich phase with a hot gas while maintaining said solid-rich phase at a temperature not higher than 100C such that said solid-rich phase is dried to have a water content of 15 % by weight or less within 60 seconds, thereby obtaining said high protein content product.
Brief Description of the Drawing Other objects, features and advantages of the present invention will become apparent from the detailed description of the preferred embodiments of the invention which follows, when considered in light of the accompanying drawing, in which:
the sole FIGURE is a schematic flow diagram showing an apparatus suitable for carrying out the process according to the present invention.
_ 3 _ ~ 21 55 042 Detailed Description of the Preferred Embodiments of the Invention BSG is constituted by husks, germs and other particles having protein contents of about 5 ~ by weight, 50 % by weight and 50 % by weight, respectively. The germs and other particles are bound to or adhered to the husks. In the present specification, the germs and other particles are commonly referred to as "proteinaceous material". BSG
separated from wort and having a water content of about 70-80 % by weight may be used as such for the purpose of the present invention. The BSG concentrated or dried for easiness in storage and transportation may also be used for the purpose of the present invention after addition of water to have a water content of at least 65 ~ by weight.
Referring now to FIGURE, BSG is fed through a line 21 to a pressing zone 1, preferably a roll mill, where BSG is subjected to pressing and shearing forces so that the proteinaceous material is scraped and separated from the husks with simultaneous grinding of the proteinaceous material. When a roll mill is used, it is preferred that the gap between rolls be 0.05-2 mm, more preferably 0.1-0.3 mm.
The BSG treated in the pressing zone 1 should contain at least 65 % by weight of water, since otherwise part of the husks which have a low protein content will be also pulverized and incorporated into the final product, so that the protein concentration of the product is lowered.
The press-ground product obtained in the pressing zone 1 is then introduced through a line 22 into a mixing zone 2, where the press-ground product is dispersed in water supplied through a line 41. The dispersing operation is performed with stirring by any suitable means such as a propeller-type stirring apparatus for a period of time sufficient to form a slurry, generally for 5-30 minutes, preferably 10-20 minutes. The water is used in an amount so that the resulting slurry has a solid matter content of 3-5 by weight, preferably 4-5 % by weight.
215SOg2 The slurry is fed through a line 23 to a first sieving zone 3 and is filtered with a sieve having a mesh size of 30-60 mesh (0.213-0.567 mm) to obtain a filtrate, in the form of a slurry, containing the ground proteinaceous material and a solid residue containing the husks. The sieve used in the sieving zone 3 is preferably of a vibrating-type.
The ground proteinaceous material generally has a protein content of 50-52 % by weight on dry basis.
The filtrate is fed through a line 30 to a first separation zone 6. Preferably, the solid residue obtained in the first sieving zone 3 is fed to a second mixing zone 4, where the solid residue is dispersed in water supplied through a line 42 to obtain a mixture, in the form of a slurry, having a solid matter content of 3-5 % by weight, preferably 4-5 % by weight. As a result of this treatment, the ground proteinaceous material remaining, in a small amount, in the solid residue is separated therefrom. The mixture is fed through a line 25 to a second sieving zone 5 and is filtered with a sieve having a mesh size of 30-60 mesh (0.213-0.567 mm) to a first phase (filtrate) which has passed through the sieve and which contains a small amount of the ground proteinaceous material and a second phase (solid residue) which has remained on the sieve and which is substantially free of the ground proteinaceous material. The first phase (filtrate) obtained in the second sieving zone 5 is fed to the first separation zone 6 through a line 26 together with the filtrate from the first sieving zone 3.
In the first separation zone 6, the filtrate from the sieving zones 3 and 5 is separated into a condensed slurry containing 0.5-2 % by weight of the ground proteinaceous material and a liquid phase. In one preferred embodiment, the separation zone 6 is a sedimentation tank or settler having a discharge port at the bottom thereof. The filtrate fed to the sedimentation tank 6 is allowed to quiescently stand for 5 minutes to 2 hours, preferably 10-20 minutes, until a condensed slurry containing 0.5-2 % by weight, preferably 1-2 % by weight, of the ground 215S0~2 proteinaceous material is formed as a result of the sedimentation. During the sedimentation, the fats (vegetable oils and fats) contained in the ground proteinaceous material is dissolved into water so that the protein concentration of the ground proteinaceous material is increased. The slurry is discharged from the sedimentation tank 6 through the bottom discharge port and is introduced into a second separating zone 7 through a line 27. The supernatant obtained in the sedimentation tank 6 is fed to the water tank 13 through lines 31 and 39.
In the second separating zone 7, the slurry is separated into a solid-rich phase having a water content of 7-95 ~ by weight, preferably 80-90 ~ by weight, more preferably 80-85 ~ by weight, and a supernatant phase by any suitable dehydrating device such as a centrifuge, a drum filter, a leaf filter or a filter press. The use of a continuous centrifuge is preferred. The protein-containing solid-rich phase is fed to a drying zone 8, whereas the supernatant is fed to the water tank 13 through lines 38 and 39.
In the drying zone 8, the solid-rich phase is brought into direct contact with a hot gas to obtain a dried product. The drying should be carried out under specific conditions, since otherwise the product is discolored or deteriorated; i.e. the product becomes dark and shows a reduced digestibility by the enzyme pepsin. Thus, it is important that the solid-rich phase should be maintained at a temperature not higher than 100C, preferably 80-90C, and should be dried so that the water content of the solid-rich phase is reduced to 15 % by weight or less, preferably 10-12 ~ by weight, in a period of 60 seconds or less, preferably in a period of 30-60 seconds. The hot gas is preferably hot air and preferably has a temperature of 300-500C, more preferably 400-450C. The drying is suitably carried out with a rotary kiln-type dryer or a drum dryer.
The dried product is discharged from the drying zone through a line 29 and is recovered. The dried product ` - 6 - _ 21S5 042 generally containing lumps is preferably ground into a particle size of 0.1-1 mm and is packaged. If desired, an anti-oxidant such as ethoxyquin (for animal feeding) or Vitamin E (for food purposes).
The solid residue (husks) obtained in the sieving zone 5 is fed to a dehydrating zone 9 through a line 32. The solid residue generally has a water content of 85 % by weight or more, typically about 91 % by weight, is thus dehydrated in the zone 9 so that the dehydrated product has a water content of less than 75 ~ by weight, typically 65-70 % by weight. A screw press, a centrifuge or a filter may be used to effect the dehydration.
The dehydrated product is then fed to a combustion zone 10 through a line 33 and is combusted. The combustion zone 10 may be, for example, a fluidized bed incineration furnace or a rotary incineration furnace. The combustion waste gas is introduced through a line 34 into a heat exchanger where the heat of the combustion waste gas is recovered by indirect heat exchange with a suitable gas medium such as air. The heated medium is fed to the drying zone 8 through a line 50 as at least part of the hot gas.
The water separated in the dehydrating zone 9 is fed to a separating zone 12, preferably a sedimentation tank, through a line 35, and is allowed to quiescently stand for 5 minutes to 2 hours, preferably 10-20 minutes, so that solids contained in the water in a small amount are separated by sedimentation to form a slurry in the bottom of the sedimentation tank. The slurry, which generally contains 0.5-1.5 ~ by weight of solid matters (husks and trace amount of the proteinaceous material), is discharged through a line 36 and recycled to the dehydrating zone 9. The supernatant obtained in the sedimentation tank 12 is fed to the water tank 13 through lines 37 and 39.
The water from the separating zones 6, 7 and 12 is collected in the water tank 13 and is recycled to the mixing zones 2 and 4 through a line 40 and the lines 41 and 42.
Excess water is discharged from the tank 13 through a line ~ - 7 _ _ 21 55 0~ 2 43, while make up water is supplied to the tank 13 through a line 44.
In the above embodiment, the second mixing zone and the second sieving zone may be omitted, if desired. In this case, the solid residue separated in the sieving zone 3 is fed to the dehydrating zone 9.
The following examples will further illustrate the present invention. Parts and percentages are by weight.
Example 1 BSG (water content: 78 ~, protein content: 25.5 %
on dry basis) was treated using the system shown in the FIGURE. Thus, 100 Kg of the BSG (dry weight 22 kg) were pressed and ground with a roll mill 1 having a roll aperture of 0.1 mm.
The ground mass was then placed in a mixing tank 2 together with 447 liters of water and stirred for 10 minutes with a propeller stirrer. The resulting slurry (solid matter content: 4 ~) was filtered with a 55 mesh sieve 3 (wire net, opening: 0.250 mm) of a vibrating type to obtain 189 kg of solid residue constituted of husks (water content: 91 %, dry weight: 17 kg) as a plus fraction and 358 liters of a filtrate in the form of a slurry (solid matter content: 1.4 %, dry weight 5 kg, protein content: 52 % on dry basis) as an under-size fraction.
The solid residue was placed in a mixing tank 4 together with 236 liters of water and stirred for 10 minutes with a propeller stirrer. The resulting slurry (solid matter content: 4 ~) was filtered with a 55 mesh sieve 5 (wire net, opening: 0.250 mm) of a vibrating type to obtain as a plus fraction and 258 liters of a filtrate in the form of a slurry (solid matter content: 1 ~, dry weight 2 kg, protein content:
47 ~ on dry basis) as an under-size fraction.
The under-size fractions (total 616 liters, protein content: 50.0 ~ on dry basis) obtained by the sieving steps 3 and 5 was fed to a settler 6 and allowed to quiescently stand for lO minutes. The sediment (condensed slurry, solid matter - 8 - _ 21 55 0~2 .
content: 2 ~) was discharged from the bottom of the setter 6 and recovered. The amount of the recovered sediment was 370 liters. The supernatant (amount: 246 liters, solid matter content: 0.1 %) was also recovered.
The sediment was found to have a protein content of 52.5 ~ on dry basis. Thus, the protein content is increased by the sedimentation. The increase is considered to be ascribed to the dissolution of lipids contained in the proteinaceous material in water during the sedimentation stage.
The condensed slurry obtained in the settler 6 was dehydrated using a centrifuge 7 (3,600 G) to obtain 38 kg of protein-containing solid-rich phase (water content: 85 ~).
The solid-rich phase was fed to a rotary hot air dryer 8 and dried for 60 seconds by contact with the hot air to obtain 6 kg of protein-rich product (water content: 10 ~). The hot air had a temperature of 440C. The solid-rich phase was maintained at a temperature below 100C throughout the drying step.
The product was then ground and sieved with a 30 Tyler mesh sieve to obtain 6 kg of a pulverized product.
This was mixed with an anti-oxidant (ethoxyquin) to obtain a mixture having an ethoxyquin content of 90 ppm. The mixture was packed in plastic bags.
The solid residue (167 kg, water content: 91 %) obtained in the sieving step 5 was dehydrated with a screw press 9 to obtain 50 kg of a dehydrated product (water content: 70 ~). The dehydrated product was burned in a rotary incinerator with kerosene oil.
Claims (10)
1. A process for the preparation of a high protein content product from brewer's spent grain containing husks and a proteinaceous material adhering to the husks, comprising the steps of:
(a) pressing the brewer's spent grain having a water content of at least 65 % by weight to separate said proteinaceous material from said husks with simultaneous grinding of said proteinaceous material;
(b) dispersing the product obtained in step (a) in water to obtain a slurry having a solid matter content of 3-5 % by weight;
(c) filtering said slurry with a sieve having a mesh size of 30-60 mesh to obtain a filtrate containing said ground proteinaceous material and a solid residue;
(d) separating said filtrate into a condensed slurry containing 0.5-2 % by weight of said ground proteinaceous material and a supernatant;
(e) separating said condensed slurry into a solid-rich phase having a water content of 70-95 % by weight and a liquid phase;
(f) contacting said solid-rich phase with a hot gas while maintaining said solid-rich phase at a temperature not higher than 100°C such that said solid-rich phase is dried to have a water content of 15 % by weight or less within 60 seconds, thereby obtaining said high protein content product.
(a) pressing the brewer's spent grain having a water content of at least 65 % by weight to separate said proteinaceous material from said husks with simultaneous grinding of said proteinaceous material;
(b) dispersing the product obtained in step (a) in water to obtain a slurry having a solid matter content of 3-5 % by weight;
(c) filtering said slurry with a sieve having a mesh size of 30-60 mesh to obtain a filtrate containing said ground proteinaceous material and a solid residue;
(d) separating said filtrate into a condensed slurry containing 0.5-2 % by weight of said ground proteinaceous material and a supernatant;
(e) separating said condensed slurry into a solid-rich phase having a water content of 70-95 % by weight and a liquid phase;
(f) contacting said solid-rich phase with a hot gas while maintaining said solid-rich phase at a temperature not higher than 100°C such that said solid-rich phase is dried to have a water content of 15 % by weight or less within 60 seconds, thereby obtaining said high protein content product.
2. A process as claimed in claim 1, further comprising the steps of dehydrating said solid residue, combusting said dehydrated solid residue to obtain a combustion waste gas, contacting said combustion waste gas with air to heat said air by indirect heat-exchange therewith, and feeding said heated air to step (f) as at least part of said hot gas.
3. A process as claimed in claim 1, further comprising dispersing said solid residue again in water to obtain a mixture having a solid matter content of 3-5 % by weight, filtering said mixture with a sieve member having a mesh size of 30-60 mesh to obtain a first phase which has passed through said sieve and a second phase which has remained on said sieve, and feeding said first phase to step (d) together with said filtrate.
4. A process as claimed in claim 3, further comprising the steps of dehydrating said second phase, combusting said dehydrated second phase to obtain a combustion waste gas contacting said combustion waste gas with air to heat said air by indirect heat-exchange therewith, and feeding said heated air to step (f) as at least part of said hot gas.
5. A process as claimed in claim 1, wherein step (a) is roll milling.
6. A process as claimed in claim 1, wherein step (d) is sedimentation.
7. A process as claimed in claim 6, wherein said sedimentation is performed by permitting said filtrate to quiescently stand for 5 minutes to 2 hours.
8. A process as claimed in claim 1, wherein step (e) is centrifugation.
9. A process as claimed in claim 1, wherein said sieve is a vibrating sieve.
10. A process as claimed in claim 3, wherein each of said sieve and said sieve member is a vibrating sieve.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6202848A JPH0838061A (en) | 1994-08-04 | 1994-08-04 | Production of high-protein dried food from beer cake as stock |
| JP6-202,848 | 1994-08-04 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2155042A1 true CA2155042A1 (en) | 1996-02-05 |
Family
ID=16464200
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002155042A Abandoned CA2155042A1 (en) | 1994-08-04 | 1995-07-31 | Process for the preparation of protein-rich product from brewer's spent grain |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JPH0838061A (en) |
| CN (1) | CN1062421C (en) |
| AU (1) | AU696577B2 (en) |
| CA (1) | CA2155042A1 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746703A (en) * | 2011-04-21 | 2012-10-24 | 长春职业技术学院 | Production method for extracting active substances from beer lees |
| EP3831212A1 (en) * | 2019-10-21 | 2021-06-09 | BioBo GmbH | Protein suspension produced from brewer's spent grain, method and apparatus for producing same |
| US11102998B1 (en) | 2017-08-25 | 2021-08-31 | The Hershey Company | Binders and methods of making and using the same |
| EP3915391A4 (en) * | 2020-04-02 | 2022-08-31 | BioBo GmbH | Protein-rich product from brewer's spent grain and method for producing same |
| WO2023100146A2 (en) | 2021-12-02 | 2023-06-08 | Duynie Holding Bv | Coarse fiber composition |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1116813C (en) * | 1999-05-28 | 2003-08-06 | 李用城 | Process for preparation of glyconitrogen and amphoteric nitrogen mixture |
| CN100366190C (en) * | 2005-11-21 | 2008-02-06 | 中国食品发酵工业研究院 | Method for producing diet fiber, feedstuff oil and protein powder simultaneously by use of wheat grains |
| JP2007244266A (en) * | 2006-03-15 | 2007-09-27 | Miyagi Prefecture | High protein-containing food and method for producing the same |
| UA98618C2 (en) * | 2006-05-19 | 2012-06-11 | Хейнекен Сеплай Чейн Б.В. | Method for producing yeast fermented beverages |
| JP2010284134A (en) * | 2009-06-15 | 2010-12-24 | Nippon Rensui Co Ltd | Method for producing purified sugar solution |
| CN101773153B (en) * | 2010-03-15 | 2011-04-20 | 山东农业大学 | Brewer's grains biscuit with high protein and dietary fibre and preparation method thereof |
| ES2484694T3 (en) * | 2011-01-27 | 2014-08-12 | Gea Mechanical Equipment Gmbh | Procedure for the processing of liquid distillation residues and device for the manufacture of a product containing proteins |
| BR112013025749B1 (en) | 2011-04-18 | 2020-01-14 | Poet Res Incorporated | systems and methods for vinasse fractionation |
| US10059966B2 (en) | 2015-11-25 | 2018-08-28 | Flint Hills Resources, Lp | Processes for recovering products from a corn fermentation mash |
| US11718863B2 (en) | 2015-11-25 | 2023-08-08 | Poet Grain (Octane), Llc | Processes for recovering products from a slurry |
| US11248197B2 (en) | 2015-11-25 | 2022-02-15 | Poet Grain (Octane), Llc | Processes for recovering products from a corn fermentation mash |
| US20180014555A1 (en) * | 2016-07-15 | 2018-01-18 | Zea10, Llc | Brewer's spent-grain based protein powder |
| US11730172B2 (en) | 2020-07-15 | 2023-08-22 | Poet Research, Inc. | Methods and systems for concentrating a solids stream recovered from a process stream in a biorefinery |
| CN113355050A (en) * | 2021-07-12 | 2021-09-07 | 武秀英 | Biological aldehyde-free glue, biological composite material and preparation method thereof |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03123479A (en) * | 1988-11-18 | 1991-05-27 | Kirin Brewery Co Ltd | Preparation of protein-rich substance, fibrous substance and/or vegetable oil from beer cake |
| JPH074170B2 (en) * | 1990-02-20 | 1995-01-25 | 麒麟麦酒株式会社 | High protein content granules derived from beer lees |
-
1994
- 1994-08-04 JP JP6202848A patent/JPH0838061A/en active Pending
-
1995
- 1995-07-31 CA CA002155042A patent/CA2155042A1/en not_active Abandoned
- 1995-08-02 AU AU28333/95A patent/AU696577B2/en not_active Ceased
- 1995-08-04 CN CN95108669A patent/CN1062421C/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746703A (en) * | 2011-04-21 | 2012-10-24 | 长春职业技术学院 | Production method for extracting active substances from beer lees |
| US11102998B1 (en) | 2017-08-25 | 2021-08-31 | The Hershey Company | Binders and methods of making and using the same |
| EP3831212A1 (en) * | 2019-10-21 | 2021-06-09 | BioBo GmbH | Protein suspension produced from brewer's spent grain, method and apparatus for producing same |
| EP3831212A4 (en) * | 2019-10-21 | 2022-03-30 | BioBo GmbH | Protein suspension produced from brewer's spent grain, method and apparatus for producing same |
| AU2019449032B2 (en) * | 2019-10-21 | 2022-12-22 | BioBo GmbH | Protein suspension from brewer's grains, method and apparatus for obtaining same |
| EP3915391A4 (en) * | 2020-04-02 | 2022-08-31 | BioBo GmbH | Protein-rich product from brewer's spent grain and method for producing same |
| WO2023100146A2 (en) | 2021-12-02 | 2023-06-08 | Duynie Holding Bv | Coarse fiber composition |
| WO2023100147A1 (en) | 2021-12-02 | 2023-06-08 | Duynie Holding Bv | Method for processing cereal grain |
| BE1029980A1 (en) | 2021-12-02 | 2023-06-26 | Duynie Holding Bv | Coarse fiber composition. |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0838061A (en) | 1996-02-13 |
| AU2833395A (en) | 1996-02-15 |
| CN1120396A (en) | 1996-04-17 |
| AU696577B2 (en) | 1998-09-10 |
| CN1062421C (en) | 2001-02-28 |
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