WO1999051782A1 - Procede de fabrication de matieres sucrees destinees a la fermentation - Google Patents

Procede de fabrication de matieres sucrees destinees a la fermentation Download PDF

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Publication number
WO1999051782A1
WO1999051782A1 PCT/JP1998/001554 JP9801554W WO9951782A1 WO 1999051782 A1 WO1999051782 A1 WO 1999051782A1 JP 9801554 W JP9801554 W JP 9801554W WO 9951782 A1 WO9951782 A1 WO 9951782A1
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WO
WIPO (PCT)
Prior art keywords
separation
lower section
raw material
section
fermentation
Prior art date
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PCT/JP1998/001554
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English (en)
Japanese (ja)
Inventor
Yutaka Tamura
Terutsugu Hori
Hiroshi Tai
Kazumi Wagatsuma
Keiji Ishii
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Ajinomoto Co., Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Ajinomoto Co., Inc. filed Critical Ajinomoto Co., Inc.
Priority to PCT/JP1998/001554 priority Critical patent/WO1999051782A1/fr
Priority to CN98806718A priority patent/CN1099466C/zh
Priority to BRPI9809714-8A priority patent/BR9809714B1/pt
Priority to MYPI99001279A priority patent/MY129273A/en
Publication of WO1999051782A1 publication Critical patent/WO1999051782A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K13/00—Sugars not otherwise provided for in this class
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase

Definitions

  • the present invention relates to a method for producing a saccharide raw material for fermentation used in various fermentation industries. More specifically, the present invention provides various useful products represented by various amino acid-producing fermentations (eg, glutamic acid fermentation, lysine fermentation) or various nucleic acid-related substance producing fermentations (eg, inosine fermentation, guanosine fermentation, inosinic acid fermentation).
  • various amino acid-producing fermentations eg, glutamic acid fermentation, lysine fermentation
  • nucleic acid-related substance producing fermentations eg, inosine fermentation, guanosine fermentation, inosinic acid fermentation.
  • Raw material used as a fermentation medium in the fermentation industry that produces quality on an industrial scale that is, starch that can be easily processed into a raw material for sugar by hydrolysis, or fermentation that can be used directly as a component of a fermentation medium
  • the present invention relates to a method of producing a sugar solution for a culture medium from various starchy raw materials without substantially producing waste by-products and minimizing the amount of water used.
  • Japanese Patent Publication No. 57-18991 discloses a method of liquefying and saccharifying raw starch materials without steaming.
  • raw starch materials such as raw sweet potato and raw sorghum are used in a cellular system.
  • the enzyme is hydrolyzed under the action of a complex enzyme preparation containing glucose, hemicellulase, pectinase, dalcoamylase, and acid-active monoamylase. Have gained.
  • Japanese Patent Application Laid-Open No. 58-141794 discloses a method for producing a concentrated sugar solution from a starchy raw material.
  • a starchy material such as potatoes
  • the liquefied starch enzyme is successively reacted with the saccharified starch enzyme in this manner, thereby producing a concentrated sugar solution.
  • Alfa-Laval Alfa-Laval Equipment for Starch Production from Fresh Manioc Roots (ALFA-LAVAL)
  • a specialized book is known, which describes that saccharification of the obtained evening power starch is used to produce a sugar solution that can be used for various uses, including for fermentation raw materials.
  • Many of the conventional techniques for separating and purifying starch from a starchy raw material or producing a sugar solution for a fermentation raw material from the obtained starch still have the following problems. That is,
  • a main object of the present invention is to solve these problems of the prior art and to provide a method for producing a so-called saccharide material for fermentation or starch which is friendly to the global environment.
  • Another object of the present invention is to provide the above-mentioned method capable of producing a sugar solution useful as a fermentation raw material by a consistent continuous process without isolating starch from a starchy raw material in the middle of the process.
  • Still another object of the present invention is to make it possible to reduce the amount of water used to the utmost by making it possible to circulate and reuse the water used in the above-mentioned continuous continuous process as appropriate between the processes, and to substantially produce by-product wastewater. Is to provide the above method that can eliminate the above.
  • Still another object of the present invention is to prevent almost all of the water-soluble sugar contained in the starchy raw material from being lost to the wastewater flowing out of the system of the production equipment without losing the water-soluble sugar.
  • An object of the present invention is to provide the above-mentioned method which can be transferred to and recovered from a raw material for fermentation saccharide as a product.
  • Still another object of the present invention is to provide a fiber fraction separated from a starchy raw material in the process of producing a saccharide raw material for fermentation, that is, containing a high concentration of easily digestible fiber, protein, or plant nutritionally useful ash.
  • An object of the present invention is to provide a method as described above, wherein solid fractions collected are collected as by-products and can be effectively used as feed for livestock, especially ruminants, or as fertilizer applied to cultivated cultivated land for producing starchy raw materials.
  • Still another object of the present invention is to transfer most of the starch and water-soluble saccharide originally contained in the starchy raw material to the target product, a fermentable saccharide raw material, at a high rate of 90% or more. It is an object of the present invention to provide the above-mentioned method which can be recovered.
  • the method for producing a saccharide raw material for fermentation from a starchy raw material according to the present invention comprises:
  • the first separated upper section that has been ground in the second grinding step is the second separated upper section.
  • the third separation upper section is led out of the system, the third separation lower section is forwarded to the inlet side of the first grinding step, and fermentation is performed from the second separation lower section. A carbohydrate raw material is obtained.
  • a starchy raw material suitable for use is a raw material derived from at least one selected from the group consisting of sago palm, rice, wheat, and corn, that is, sediment collected from the above-ground growth site of a cultivated crop plant. It is a raw material with little contamination.
  • the method further comprises a solid-liquid separation step of separating the solid section from the second lower separation section.
  • the method further comprises a washing step of washing the starch material with water prior to the first grinding step, wherein the washing step includes circulating washing water, Is subjected to a purification treatment for separating and removing contained solid matter during the circulation process.
  • the starchy raw material suitable for use is a raw material derived from at least one selected from the group consisting of cassava, potato, and sweet potato, i.e., collected from an underground growth site of a cultivated crop plant, such as soil and sand. It is a raw material that may be mixed.
  • the second separation step and Z or the third separation step are preferably performed according to a compressed floating separation method (Compressed Floating Separation).
  • the method comprises a hydrolysis step of liquefying and saccharifying the second separation lower section; and a relatively light fourth separation upper section for separating the product from the hydrolysis step. Further comprising a fourth separation step of separating the fraction from the heavy fourth separation lower section, wherein the fourth separation upper section is led out of the system and is a fermentation sugar which is a target product.
  • the raw material is obtained as a sugar liquid from the fourth separation lower section.
  • the fourth separation step is preferably performed according to a filtration and / or centrifugation method.
  • a method for producing a saccharide raw material for fermentation from a starchy raw material comprises:
  • the third separation upper section is led out of the system, the third separation lower section is sent to the inlet side of the first grinding step, and the fermentation saccharide as a target product is provided.
  • Raw materials are obtained from the second separated lower section.
  • the starchy raw material used here is preferably a raw material derived from at least one selected from the group consisting of sago palm, rice, wheat, and corn, that is, collected from the above-ground growth site of the cultivated crop plant. It is a raw material with little contamination such as earth and sand.
  • the method according to this another aspect may further comprise a step of separating the solid section from the second separation lower section.
  • the second separation step is preferably performed according to a pressure floating separation method
  • the third separation step is preferably performed according to a solid-liquid separation method such as filtration.
  • the above method may further include a step of allowing the second separation lower section to settle and settle, and in this case, the supernatant liquid after the settling and settling is sent to the second separation step as separation water, and Certain fermentable carbohydrate raw materials are obtained from a second settled lower section that has settled down.
  • a hydrolysis step of liquefying and saccharifying the second separation lower section may further include a fourth separation step of separating a product from the water splitting step into a relatively light fourth separation upper section and a heavy fourth separation lower section.
  • the separated upper section is led out of the system together with the third separated upper section, the fiber section is obtained as a by-product of feed or fertilizer, and the target saccharide raw material for fermentation is the 4th separated upper section. Obtained as a sugar solution from the lower separation section.
  • said fourth separation step is performed according to a filtration or centrifugation method.
  • the method may further comprise one or more additional separation steps of separating the second separation lower section into a relatively light additional separation upper section and a heavy additional separation lower section, wherein: The additional separation upper section is introduced into the third separation step, and the target product, a saccharide raw material for fermentation, is obtained from the additional separation lower section.
  • the method may further comprise a step of separating the solid fraction from the additional separation lower section, and the additional separation step is preferably performed according to a pressurized flotation method.
  • the method further comprises: a hydrolysis step of liquefying and saccharifying the additional separation lower section; and separating the product from the hydrolysis step into a relatively light fourth separation upper section and a heavy fourth separation lower section.
  • the fourth separation upper section is led out of the system, and the fermentation saccharide raw material that is the target product is the fourth separation lower section. Obtained as a sugar solution.
  • a raw material derived from sago palm is specifically used as the starchy raw material. That is, starchy raw materials derived from sago palm have conventionally been regarded as raw materials in which contaminants such as fibers are likely to be mixed into the final carbohydrate product.
  • starchy raw materials derived from sago palm have conventionally been regarded as raw materials in which contaminants such as fibers are likely to be mixed into the final carbohydrate product.
  • a multi-stage separation process it is possible to obtain a high-quality sugar solution from which impurities such as fibers are completely removed as a raw material for fermentation sugar, which is the target product.
  • the carbohydrate raw material for fermentation produced by the method of the present invention is a sugar liquid used as a main component of a culture medium in various fermentation applications and a starch which is a main raw material of the sugar liquid.
  • the sugar product or sugar solution for fermentation which is the target product obtained in the present invention, can be used for a wide variety of fermentations without any particular limitation on the type of fermentation. It is suitable for use in, for example, glutamic acid fermentation, lysine fermentation, or fermentation for producing various nucleic acid-related substances, for example, inosine fermentation, guanosine fermentation, for example, inosine acid fermentation.
  • the fermentation saccharide raw material obtained by the method according to the present invention in fermentation other than these, for example, fermentation for producing pharmaceuticals such as antibiotics, alcohol fermentation, and brewing of alcoholic beverages is a high-quality sugar liquid raw material that gives good results. It can be used, and in that case, no remarkable trouble is found in such use.
  • the starchy raw material used as a main starting material in the method of the present invention is not particularly limited as long as it is an agricultural and forestry product containing starch at an appropriate concentration and preferably can be supplied in a large amount and stably, and a processed product thereof. Can be used.
  • the starchy raw material may be in any form such as seeds, rhizomes, underground roots, stem accumulations, and may be a fresh product immediately after being harvested from the cultivated arable land, or may be dehydrated, washed, It may be a semi-finished or processed product that has undergone preliminary processing such as drying, air drying, cutting, steaming, freezing, crushing, and grinding. Further, the starchy raw material may be not only a starchy product after the purification treatment but also a crude raw material containing a considerable amount of components or impurities other than starch.
  • starchy raw material there are raw materials containing carbohydrates other than starch, for example, a water-soluble sugar at a considerable concentration, but in the method according to the present invention, even a water-soluble sugar is a target product. It is incorporated into the sugar raw material (sugar solution) for fermentation and can be used without any excess.
  • sugar raw material sucgar solution
  • the conventional method for producing starch or the method for producing a sugar solution after separating starch all the water-soluble sugar contained in the starch raw material width is discharged together with wastewater during the production process, and is disposed of. It had been.
  • starchy raw materials that can be used in the present invention are listed below according to the crop plant from which they are derived.
  • A Example where the main location of starch is above ground
  • Potato raw potato Potato frozen cut dried, Potato whole lump peeled frozen dried product, Potato potato powder B3) From sweet potato:
  • Sweet potatoes Sweet potatoes, Sweet potatoes, Sweet potatoes, Sweet potato flour
  • the method according to the present invention includes two grinding steps of the first grinding step and the second grinding step in the series of steps.
  • the grinding method and the equipment used in these grinding steps there is no particular limitation on the grinding method and the equipment used in these grinding steps, and various known grinding methods and equipment can be used. For example, grinding methods and equipment using rotating stones are the most common. It is possible to use it.
  • the grinding treatment may be performed in a single stage or in multiple stages.
  • the method according to the present invention in a series of steps, at least three separation steps of a first separation step, a second separation step and a third separation step, preferably a total of four separation steps further including a fourth separation step, More preferably, it comprises five or more separation steps with one or more additional separation steps.
  • a process to separate and acquire the relatively light upper separation section and the heavy separation lower section in the section to be separated is performed.
  • the lighter separation upper section contains more fiber components and the heavier separation lower section contains more starch or saccharified glucose.
  • an appropriate separation method and apparatus can be used according to the form of the section to be separated and the purpose of the separation, for example, wet sieving, passage through a strainer, centrifugation, filtration, static
  • a suitable method may be selected from separation methods such as sedimentation and equipment, and used.
  • the second separation step and the additional separation step it is preferable to apply a separation treatment by a pressure flotation method.
  • the pressure flotation method is used when separating the first separation upper section ground in the second grinding step, and the second separation step is performed in the second grinding step.
  • a solid-liquid separation method such as filtration.
  • the liquid after the starch hydrolysis is separated into an upper separation section containing fine fiber components and a lower separation section which is a highly viscous saccharified liquid produced by hydrolysis.
  • filtration, pressure filtration or high speed continuous liquid centrifugation such as the use of a Sharpless centrifuge, is particularly suitable.
  • air bubbles are generated at the bottom of a tank containing a liquid in which fine solids are dispersed.
  • Pressurized gas is introduced through the nozzle, and while the bubbles ejected from the nozzle float in the liquid, fine solids in the liquid adhere to the surface of the bubbles, causing the bubbles to float.
  • Fine solids adhering to the surface of the bubbles are brought to the surface of the liquid along with the top, and fine solids are spilled over the upper edge of the side wall of the tank to the outside due to the lump of air bubbles. It is discharged outside and separated.
  • This pressurized flotation method has been used in similar ways to purify wastewater or beneficiation in mines, but few examples have been applied to starch production or related technical fields. .
  • each of the upper separation sections resulting from the third and fourth separation steps contains a large amount of fiber components, but has a low starch or sugar content, so that it is out of the system as a by-product.
  • These derived upper separations can be used as livestock feed or fertilizer for each separation step or for both separation steps together. Therefore, the by-product derived outside the system by the method of the present invention is not a waste but a resource that can be effectively used.
  • the third separation lower section generated in the third separation step is a liquid still containing a saccharide useful for the target product, such as a starch or a sugar solution.
  • the third separation lower section is sent to the first grinding step, where it is reused for the required grinding water.
  • the supernatant liquid resulting from the solid-liquid separation may contain some starch.
  • it is a dilute dispersion containing fibers, the entire amount of these supernatants is also circulated to the inlet side of the immediately preceding separation step and reused.
  • the separation supernatant liquid generated inside the series of steps is itself of low utility value, it is circulated and reused between the steps, thereby achieving the entire process. It is possible to remarkably reduce the amount of water used in the above. Also, useful substances such as starch contained in these liquids or easily water-soluble sugars contained in the raw materials of starch are introduced into the process again without being discharged into the system and discarded. The components are available with almost complete efficiency. Therefore, there will be almost no waste generated from each separation step.
  • the fourth separation lower section generated from the fourth separation step is a section of the sugar liquid itself as a fermentation saccharide raw material which is a target product.
  • This category contains not only glucose produced by hydrolysis of starch, but also water-soluble sugars contained in the starting starchy material, especially water-soluble sugars. All sugars are accumulated in a concentrated manner without being leaked out of the system and discarded in the middle of the process.
  • the water-soluble sugar contained in the starchy raw material is discharged out of the system during the treatment process, and the biological oxygen demand (B0D) in the surrounding environment is reduced. Although it did not cause much increase in the amount of water and caused environmental pollution, in the method of the present invention, not only the starch contained in the starchy raw material but also the water-soluble sugars were completely produced without any excess. Since it is collected in waste, there is no place to generate any waste that causes environmental pollution.
  • the second separation lower section resulting from the second separation step, or the additional separation lower section obtained by subjecting the second separation lower section to one or more additional separation steps, or furthermore, these separation lower sections are allowed to stand and settle.
  • the sedimentation section obtained by the treatment is a section mainly composed of starch separated from the starchy raw material. From these lower sections, starch can be separated and obtained by an appropriate solid-liquid separation method, or this lower section can be directly subjected to hydrolysis treatment to be processed into a sugar liquid as a sugar material for fermentation. can do. Either a strong acid hydrolysis method or an enzymatic hydrolysis method can be used for the hydrolysis treatment. However, in general, from the viewpoint of using the produced sugar solution as a raw material for fermentation, and from the viewpoint of the convenience of the treatment operation, it is generally used. Employs an enzymatic hydrolysis method.
  • this method comprises a liquefaction step in which starch is subjected to Hi-amylase as a starch liquefying enzyme, and a saccharification step in which glycamylase acts as an enzyme for saccharifying the liquefied starch to produce an easily fermentable sugar such as glucose. And is included.
  • Enzymatic hydrolysis maintains a high reaction rate and contaminates the process due to various bacteria.
  • the sugar solution obtained as a raw material for fermentation carbohydrate obtained through the hydrolysis treatment step can be supplied to the fermentation step directly as it is or after being concentrated to an appropriate concentration as a fermentation medium.
  • the distance from the point of production of the sugar solution for fermentation sugar material to the fermentation plant is remote, or when the sugar solution for fermentation sugar material is produced, it is accumulated and then the fermentation process is started.
  • the sugar solution may be transported or stored after being concentrated to a concentration suitable for the fermentation medium.
  • the starchy raw material is washed with water before being introduced into the first milling step.
  • the washing water used in this washing step is circulated and used, and the accompanying solid matter is removed by purification treatment in the course of the circulation path to become clean water. That is, according to the present invention, the starchy raw material is once cleaned with the cleaning water that is used in the cleaning step to purify the water used in the cleaning step and circulate again. Therefore, even in the washing process, the amount of washing water used can be reduced to the minimum required.
  • the purification equipment installed in the circulation path includes any equipment capable of solid-liquid separation, such as a settling tank, a strainer, and a filtration net.
  • the solid matter mixed or attached to the starch raw material physically moves into the washing water and is separated and removed from the raw material.
  • These solids include, for example, in the case of starchy raw materials consisting of underground growth sites such as cassava, potato or sweet potato, soil, sand, mud, or skin peeled off from raw materials mixed with or attached to raw materials And so on.
  • washing water used in the washing process or the grinding water used in the first grinding process is the water that circulates in the system as mentioned above. Safe new water such as water is replenished.
  • FIG. 1 is a flowchart showing a flow of a method for producing a saccharide raw material for fermentation according to one embodiment of the present invention.
  • FIG. 2 is a process chart showing a flow of a method for producing a saccharide raw material for fermentation according to another embodiment of the present invention.
  • the starchy raw material SM is first washed with washing water WW in a washing step WS.
  • the cleaning water W after the cleaning is subjected to a purification process in the purification process PR, solids SS are removed from the cleaning water out of the system, and the cleaning water thus purified is again provided for cleaning.
  • the washed raw material SM is sent to the first grinding step G1 and is ground under water.
  • the water WG used in this grinding step is the entire amount of the third separation lower section SPL3 generated from the third separation step S3 described later in the process system, and if it is insufficient, additional water WA is supplied from outside the system.
  • the raw material sufficiently finely ground in the first grinding step G1 is sent to the first separation step S1, where it is divided into a relatively light first separation upper section SPU1 and a relatively heavy first separation lower section SPL1.
  • First Separation Upper Section SPU1 is mainly composed of fibrous material, which still contains small amounts of starch and sugar.
  • the first separated lower section SPL1 contains a small amount of solid matter, but is mostly a liquid containing a large amount of starch and sugar.
  • the first separation upper section SPU1 is sent to the second grinding step G2 and is ground again, while the first separation lower section SPL1 is sent to the second separation step S2 and the relatively lighter second separation upper section It is separated into Category SPU2 and a relatively heavy second separation lower Category SPL2.
  • Most of the solids contained in the first separation lower section SPL1 have been transferred to the second separation upper section SPU2, and the second separation lower section SPL2 is included in the first separation lower section SPL1.
  • Most of the starch and sugars that have been transferred have been transferred.
  • 3rd Separation Upper Section SPU3 has a low starch or sugar content but a high fibrous content, so it is extracted out of the system as a by-product BP and used as livestock feed or fertilizer.
  • the third separation lower section SPL3 is a liquid that does not contain fiber but contains a small amount of sugar, and is circulated to the first grinding step G1 as grinding water and reused.
  • the second separation lower section SPL2 contains high concentrations of starch and sugar, so when starch is directly obtained from it, it is sent to the solid-liquid separation process SE by filtration or centrifugation, etc., and the starch cake or solid starch ST is obtained. Is obtained.
  • the second separated lower section SPL2 is sent to the hydrolysis step HY.
  • the hydrolysis step HY liquefaction and saccharification of starch are performed by an enzyme, and the decomposition product solution is sent to a fourth separation step S4 by filtration or centrifugation.
  • the decomposition product liquid is separated into a fourth separation upper section SPU4, which is mostly solid matter and hardly contains saccharides, and a fourth separation lower section SPL4 as a high-quality sugar solution.
  • the fourth separated upper section SPU4 is led out of the system together with the third separated upper section SPU3 as a by-product BP and is effectively used as feed or fertilizer.
  • the target product, the fermentation carbohydrate raw material FM is obtained from the fourth separation lower section SPL4.
  • the fourth separation lower section SPL4 is obtained as the sugar liquid FM concentrated in the concentration step CC as necessary. I have.
  • a clean starchy raw material SM with almost no dirt is used.
  • the starchy raw material SM is directly finely ground in the first grinding step G1, and then separated in the first separation step S1 into the same first separation upper section SPU1 and first separation lower section SPL1 as described above. .
  • the first separation lower section SPL1 is further finely ground in the second grinding step G2, and then separated into the second separation upper section SPU2 and the second separation lower section SPL2 in the second separation step S2.
  • the second separation lower section SPL2 is subjected to standing sedimentation treatment D1 for an appropriate time, and the supernatant SNS1 is refluxed to the inlet side of the second separation step S2.
  • the second separation lower section SPL2 that has passed through the stationary sedimentation treatment D1 passes stepwise through the first additional separation step SA and the second additional separation step SB. That is, the additional separation upper sections SPUA and SPUB generated from each additional separation step SA and SB are sent to the third separation step S3 together with the first separation upper section SPU1 and the second separation upper section SPU2, while the first additional separation step
  • the additional separation lower section SPLA generated from SA is sent to the second additional separation step SB via the stationary settling process D2 at the back, and the additional separation lower section SPLB generated from the second additional separation step SB is set at the downstream. Settlement treatment sent to D3.
  • the supernatant SNS2 generated in the stationary sedimentation treatment D2 is returned to the inlet side of the first additional separation step SA, and the supernatant SNS3 generated in the stationary sedimentation treatment D3 enters the second additional separation step SB. Recirculated to the side.
  • the first separation upper section SPU1, the second separation upper section SPU2, and the additional separation upper sections SPUA and SPUB merge to form the third separation upper section SPU3 of the solid section by solid-liquid separation.
  • a third separation lower section SPL3 of the liquid section As in the embodiment shown in FIG. 1 described above, the third separated upper section SPU3 is led out of the system as a by-product BP that is effectively used as feed or fertilizer, and the third separated lower section SPL3 is Grinding process It is recycled in the system as water for G1.
  • the second separation lower section SPL2 passes through a plurality of additional separation processes SA and SB and the stationary sedimentation treatment D1, D2, D3, and passes through the final stationary sedimentation treatment D3. And separated into upper section DCU3 containing sugar and sugar and lower section DCL3 containing relatively high concentrations of starch and sugar.
  • This upper section DCU3 is circulated in the system together with the third separation lower section SPL3 as water for the first milling process Gl, while the lower section DCL3 contains high concentrations of starch and sugar, and therefore will be directly When starch is obtained, it is sent to a solid-liquid separation step SE by filtration or centrifugation to obtain a starch cake or solid starch ST.
  • the second separated lower section SPL2 is sent to the hydrolysis step HY.
  • liquefaction and saccharification of starch are performed by an enzyme, and the decomposition product stream is sent to a fourth separation step S4 by filtration or centrifugation.
  • the decomposition product stream is separated into a fourth separation upper section SPU4, which is mostly solid matter and contains almost no saccharide, and a fourth separation lower section SPL4 as a high-quality sugar solution.
  • the fourth separated upper section SPU4 is led out of the system together with the third separated upper section SPU3 as a by-product BP and is effectively used as feed or fertilizer.
  • the target product, the fermentation carbohydrate raw material FM is obtained from the fourth separation lower section SPL4.
  • the fourth separation lower section SPL4 is obtained as the sugar liquid FM concentrated in the concentration step CC as necessary. I have.
  • a sugar solution useful as a sugar raw material for fermentation was produced from raw potatoes of cassava produced by Mas-Ija, Indonesia, as described below, in a semi-continuous process.
  • WS Cleaning process
  • Fresh cassava potatoes (manioc roots) were weighed immediately after harvest from the field, and about 1050 kg of the potatoes were poured into the washing basket of the washing tank and washed continuously.
  • the washing basket has a large number of holes in the wall and is a cylindrical iron plate that rotates in the washing water.
  • Table 1 shows the contents of starch, reducing sugar (denoted as D-sugar), protein, lipid, crude fiber, ash and moisture in the green cassava after washing.
  • the analysis method for each component was the same as that for commonly used starch-related products.
  • tap water was initially used for the washing water WW, but after the supply of washing water was balanced, the water recovered from the washing tank was purified by the purification device PR and circulated and supplied to the washing tank. , Reused. That is, the water after washing the potatoes in the washing tank is led to a conical bottom settling tank arranged in the circulation system, and then a two-stage metal grid type with a grid spacing of 10 and 5 thighs The sludge is passed through a strainer, where the mud contained in the washing water and solid matter SS such as potato skin peeled off from the surface of the raw potatoes are separated, whereby purified water WW is supplied again to the washing tank.
  • a strainer where the mud contained in the washing water and solid matter SS such as potato skin peeled off from the surface of the raw potatoes are separated, whereby purified water WW is supplied again to the washing tank.
  • the potatoes after the washing treatment were weighed again, and 1000 kg thereof was subjected to a grinding treatment.
  • the raw potatoes were first cut into slices using a large slicer, and then the cut raw potato slices were ground using a rotary mill-type grinding device under the supply of grinding water. .
  • the tissue of the raw potato is obtained as a completely collapsed paste-like raw potato pulp, which can pass through a strainer with a grid spacing of 5 hires installed at the outlet of the grinding device. there were.
  • the total amount of service water supplied during the grinding process is 1800 kg, of which 710 kg is tap water newly supplied, and the remaining 1090 k is the third lower separation section SPL3 circulated from the third separation step S3 described later.
  • the water for grinding was adjusted to be continuously supplied at a weight of about 1.5 to 2.0 times the raw potato slices.
  • the amount of raw potato pulp obtained after the grinding treatment was 2800 kg. lc) 1st separation step (SI)
  • First grinding step Raw potato pulp obtained by grinding in Gl was continuously subjected to a first separation step S1.
  • a wet sieving device was used for this separation, and the grid spacing of the used sieves was 4 mm.
  • Table 2 shows the sieved material obtained in the first separation step S1, that is, the first separated upper section SPU1 containing a large amount of potato bark fiber and the like, and the slurry that passed through the sieve, that is, the first separated lower section SPL1, The yield (kg), distribution rate, classification yield (kg), starch concentration) and total solid content (%) of each component are shown. Table 2
  • the yield is a value obtained by processing 1000k of starch raw material.
  • the slurry-like first separation lower section SPL1 obtained through the sieve in the first separation step S1 was continuously subjected to the second separation step S2.
  • a pressure flotation device was used for separation.
  • the pressurized flotation separator includes a separation tank and an overflow tank surrounding the separation tank, and a nozzle having a number of holes is arranged at the bottom in the separation tank.
  • the slurry-like first separation lower section SPL1 was fed into the separation tank, and pressurized air was supplied to the nozzle at the bottom of the separation tank.
  • a relatively light second separation upper section SPU2 floats along with bubbles ejected from a number of nozzle holes, and the floating second separation upper section SPU2 is separated.
  • the second separation upper section SPU2 obtained in the overflow tank contained a large amount of potato bark fiber and the like, and was a gray-white fibrous material as a whole.
  • the second separation lower section SPL2 remaining in the separation tank was a white or light yellow-brown starch slurry in a wet state.
  • Table 3 shows the yield (kg), distribution rate, classification yield (kg), and distribution of each component for the second separation upper section SPU2 and the second separation lower section SPL2 obtained in the second separation step S2. The starch concentration (%) and the total solid content (%) are shown.
  • the yield is the value when 1,000 kg of starch material is treated
  • the sieved material obtained in the first separation step S1, that is, the first separation upper section SPU1 contains a large amount of potato bark fiber and the like.Therefore, the first separation upper section SPU1 is again subjected to the grinding using a rotary stone type grinding machine. Grinding was performed until the tissue of the potato fiber was completely disintegrated to give a fine pulp. The obtained product was refined enough to pass through a strainer with a lattice spacing of 3 mm installed at the outlet of the grinding device.
  • the second grinding step G2 was refined.
  • the first separation upper section SPU1 and the aforementioned second separation upper section SPU2 were combined and subjected to a third separation step 3S.
  • a pressurized flotation apparatus having the same configuration as described above was used.
  • the pressurized air having a higher pressure is supplied to a larger number of nozzle holes having a smaller diameter than in the case of the second separation step S2.
  • the relatively light third separation upper sediment white section SPU3 which was relatively light, floated along with the rise of the bubbles, and steadily climbed over the upper edge of the separation tank and overflowed into the overflow tank.
  • a relatively heavy third separation lower section SPL3 remained in the separation tank, and this lower section settled and separated at the bottom of the separation tank when the supply of pressurized air was interrupted.
  • the majority of the SPU3 in the third separation upper section is fine fiber derived from 4 potato skins.
  • Table 4 shows the yields (kg), distribution ratios, and total yields (kg) of each component of the third separation upper section SPU3 and the third separation lower section SPL3 obtained in the third separation step S3. ), Starch concentration) and total solid content (%).
  • the yield is the value when 1,000 kg of starch material is treated
  • the second separation lower section SPL2 obtained in the second separation step S2 is the starch separated from the raw material. Is a slurry-like category containing a large amount and high concentration of The second separation lower section SPL2 was heated to 93 ° C to 97 ° C with stirring and with the addition of heat-resistant heat-amylase liquefying enzyme (Kristase T-5, trade name: 5500u / g). Liquefied. Thereafter, the temperature of the solution was lowered to 60 ° C, and glucoamylase saccharifying enzyme (trade name: Gluczym NL 4.2, titer: 4200u / g) was added in an amount equivalent to 0.07% (3u) in terms of the weight ratio to starch.
  • heat-resistant heat-amylase liquefying enzyme Keristase T-5, trade name: 5500u / g. Liquefied. Thereafter, the temperature of the solution was lowered to 60 ° C, and glucoamylase
  • the saccharified solution obtained in HY is filtered using a filter cloth made of polypropylene mixed spinning, and the 4th upper separation SPU4 as a filter cake remaining on the filter cloth and the filtrate passed through the filter cloth And SPL4.
  • the fourth upper division SPU4 contains fine fibrous substances and brown proteinaceous substances, and the fourth lower division SPL4 is a pale yellow sugar solution.
  • Table 5 shows the fourth separation upper section SPU4 containing a large amount of fine fibers and the like obtained in the fourth separation step S4 and the fourth separation lower section SPL4 of the target product sugar solution (sugar raw material for fermentation).
  • the yield (kg), distribution rate, total yield (kg), and glucose concentration (5 and total solid content (3 ⁇ 4)) of each component are shown.
  • the yield is the value when 1,000 kg of starch material is treated
  • the fourth separation lower section SPL4 was concentrated to about 60% volume under a weak reduced pressure.
  • This concentrated sugar solution FM can be used as a fermentation sugar raw material for fermentation of various amino acids such as glutamic acid-producing fermentation or fermentation of nucleic acid-related substances such as nucleosides and nucleotides.
  • the third separation lower section SPL3 which is slightly turbid due to the presence of a small amount of starch etc., is recirculated from the third separation step S3 to the first grinding step G1 and supplied as water to the rotating millstone-type grinding equipment in operation Was done. lk) Derivation / effective use of by-product BP
  • the third separation upper section SPU3 and the fourth separation upper section SPU4 contain a large amount of potato bark fiber and the like refined by the preceding grinding treatment, and as shown in Tables 4 and 5, unrecovered Contains starch, D-sugar, protein, etc.
  • Table 6 shows the yield and composition ratio of each component of the mixture BP obtained by combining these two separated upper sections SPU3 and SPU4.
  • this mixture can be effectively used as feed for livestock, especially feed or feed additives for ruminants such as red oaks and sheep. It is also useful as a feed additive for monogastric animals such as bush.
  • the third separation upper section SPU3 and the fourth separation upper section SPU4 are obtained in a wet state whether individually or mixed. When used as feed, it can be used in the wet state as obtained, or it can be used after being subjected to appropriate dehydration and drying treatments and then stored and matured as necessary.
  • the 3rd upper separation section SPU3 and 4th upper separation section SPU4 are also useful as fertilizers for cultivated plants or as raw materials for individual divisions or as a mixture. Available. As shown in Table 6, they contain a significant concentration of ash and are therefore particularly useful as fertilizers applied to cassava fields.
  • Table 7 shows the overall yield of each component in the method of this example, which goes through a series of the first grinding step G1 and the second grinding step G2 and the first separation step S1 to the fourth separation step S4. Shown in Table 7 shows the yield of each component not only for the sugar product FM, which is the target product, but also for the by-product BP used in feeds and the like.
  • Glucose-minic acid fermentation was carried out using the sugar solution FM obtained as described above as a carbohydrate raw material for fermentation, and it was derived from other starchy raw materials that were conventionally used at the actual production scale. It has been confirmed that glucuramic acid can be produced preferably while maintaining a sugar yield and a glucumic acid accumulation concentration in the medium that are equal to or higher than those obtained when using a sugar raw material for fermentation, for example, a sugar solution derived from cane molasses. Was done.
  • the sagobis was peeled off from the sago palm trunk immediately after logging, the starch-containing portion of the sagobis was separated, and the contaminated bark and wood chips were removed.
  • Starch contained in fractionated Sagobis Table 8 shows the composition ratio (3 ⁇ 4) of flour, fiber and moisture and the composition weight (kg) per 1000 kg.
  • the milled sagobis was in the form of pulp, and the composition and weight of the main components contained in it were as shown in Table 9.
  • the sagobis pulp was sieved and separated by a wet sieve to obtain a first separated upper section SPU1 containing coarse fibers such as hulls and a first separated lower section SPL1 containing starch. still, The effective sieve slit interval of the used wet sieve was 0.12.
  • Table 10 shows the composition ratios and weights of starch, fiber, and water contained in the upper and lower separation sections SPU1 and SPL1 obtained in the first separation step S1.
  • the first separation lower section SPL1 is ground again by a rotary stone type grinding device in which the grinding surface is more finely adjusted than the grinding device used in the first grinding process G1, The starch particles contained in the fiber structure were released from the fiber structure.
  • Second grinding step The fine first separation lower section SPL1 further ground in G2 is separated by pressure flotation, and mainly contains the light second separation upper section SPU2 containing fibers and mainly starch 2nd Separation Lower Division SPL2 was separately acquired.
  • This second separation lower section SPL2 was further subjected to stationary sedimentation treatment D1, and the supernatant SNS1 generated there was recirculated and reused in the pressurized flotation separation treatment in the second separation step S2.
  • the amount of water circulated to the second separation step S2 was 10620 kg (three times the amount of liquid introduced from the second grinding step G2).
  • Table 11 shows the component ratios and weights of the components contained in the upper and lower separation sections SPU2 and SPL2 obtained in the second separation step S2.
  • the second separation lower section SPL2 is allowed to stand still and sedimentation treatment
  • the sediment-containing liquid obtained through D1 is subjected to separation processing again by the pressure flotation method, and the first additional separation section containing fibers
  • the first addition including SPUA and starch Separated lower section SPLA was obtained.
  • the amount of the sediment-containing liquid introduced from the stationary sedimentation treatment D1 was 2996 kg
  • the water content was 2713 kg
  • the water for pressurized flotation treatment in the first additional separation process SA was
  • the supernatant SNS2 generated from the stationary sedimentation treatment D2 was refluxed and reused.
  • the amount of water circulated to the first additional separation step SA was 8987 kg (three times the amount of the sediment-containing liquid introduced from the second separation step S2).
  • Table 12 shows the composition ratio and weight of the components contained in SPUA and SPLA.
  • Composition ratio Weight (kg) Composition ratio (50 Weight (kg)
  • First additional separation lower section SPLA is allowed to stand still, and the sediment-containing liquid obtained by passing through D2 is subjected to further separation treatment by pressurized flotation, and the second additional separation upper section containing fibers SPUB and starch containing starch 2 Additional separation lower section SPLB was acquired.
  • the amount of the sediment-containing liquid introduced from the stationary settling treatment D2 in the former stage was 2525 kg, the water content was 2289 kg, and the water for pressurized flotation treatment in the second additional separation process SB was added to the latter stage.
  • the supernatant SNS3 generated in the stationary sedimentation treatment D3 was refluxed and reused.
  • the second additional separation step refluxing was water amount in the SB is 7576Kg c was (first additional separation 3 times the process has been introduced from the SA sediment-containing liquid volume) the second additional isolation lower section SPLB, subsequent The fiber was almost completely removed to the extent that the process did not interfere.
  • Table 13 shows the composition ratio and weight of the SPUB and SPLB components in both upper and lower separation sections after SB.
  • Second additional separation lower section SPLB was further passed through a stationary sedimentation treatment D3 to be separated into a settling separation upper section DCU3 (almost all of water) and a settling separation lower section DCL3 (starch slurry).
  • the total volume of the second additional separation section was 2,213 kg, of which the water content was 2008 kg.
  • the starch in the sedimentation-separation lower section (starch slurry) DCL3 was 71.4% of the starch in the starting material Sagobis.
  • heat-resistant heat-amylase liquefying enzyme trade name: Krystase T-5, titer: 5500 u / g. It was liquefied by steam heating to 97 ° C. Thereafter, the temperature of the solution was lowered to 60 ° C, and glucoamylase saccharifying enzyme (trade name: Dalkzy
  • the temperature of the enzyme reaction system was maintained within the range of 55 ° C to 60 ° C, and light stirring was continued. After about 48 hours, the starch granules were completely dissolved and disappeared. Next, it was confirmed that the sugar concentration in the reaction system had reached a predetermined value, and a starch liquefaction reaction and a saccharified solution in which the saccharification reaction had been completed were obtained.
  • the saccharified solution obtained in HY is filtered while hot using a nylon-blend filter cloth, passed through the fourth separation upper section SPU4 consisting mainly of fibers remaining on the filter cloth, and the filter cloth And the fourth filtrate SPL4 as the separated filtrate was obtained separately.
  • the fourth upper division SPU4 contains fine fibrous substances and brown proteins, and the like, and the fourth lower division SPL4 is a pale yellow sugar solution.
  • Table 15 shows the components of the 4th separation upper section SPU4 obtained in the 4th separation step S4 and the 4th separation lower section SPL4 of the sugar product (sugar raw material for fermentation) that is the target product. (Kg), distribution rate, total yield (kg), glucose concentration) and total solids content (%) of the product.
  • the fibers remaining in the fourth separation lower section SPL4 were only 0.2% or less of the fibers in the starting material Sagobis.
  • the 4th separation lower section SPL4 was concentrated to about 60% volume under weak reduced pressure to obtain the target product, a sugar solution FM as a sugar material for fermentation.
  • the first separation upper section SPU1, the second separation upper section SPU2, the first additional separation upper section SPUA and the second additional separation upper section SPUB are mixed to form a mixture MX, and the mixture MX is subjected to the third separation step S3. Introduced.
  • Table 16 shows the composition ratio and the weight of the components contained in the mixture MX.
  • the mixture MX was sieved with a wet rotary sieve to obtain a third separation upper section SPU3 and a third separation lower section SPL3.
  • the effective sieving interval of the wet rotary sieve is 0.089.
  • Table 17 shows the composition ratios and weights of the components contained in the upper and lower separation sections SPU3 and SPL3 after the third separation step.
  • the third separation upper section SPU3 and the fourth separation upper section SPU4 were mixed and led out of the system to obtain by-product BP.
  • This by-product BP is mainly composed of finely divided fibers, contains starch and sugar (glucose), and is wet, or after drying, feed, especially ruminant feed, or fertilizer, especially tropical. It is effectively used as a fertilizer for crops.
  • Table 18 shows the component ratios and weights of the by-products BP (mixture of SPU3 in the third separation upper section and SPU4 in the fourth separation upper section).
  • the starch contained in this by-product was 5.7% of the starting material Sagobis starch, and the fiber content was 91.0% of the raw material Sagobis fiber. It was observed that some of the fibers had migrated to this by-product.
  • the third separation lower section SPL3 which is slightly turbid due to the presence of a small amount of starch etc., flows from the third separation step S3 to the first grinding step G1, where it is used by the operating rotary stone for the type grinding equipment. Supplied as In addition, the sedimentation separation upper section DCU3 obtained from the final standing sedimentation treatment D3 was also returned to the first grinding step G1 and reused as grinding water. DCU3, the upper part of the final sedimentation sedimentation treatment, was mostly water, and its amount was 1530 kg. SPL3, the third lower section, consisted of 62 kg of starch, 8 kg of fiber, and 2548 kg of water. The starch and fiber present in the starting material sagobis were mixed into the grinding water at a ratio of 22.9 and 8.8%, respectively, and were refluxed.
  • the sugar solution FM obtained as described above is comparable to the conventional method using cane molasses in sugar production FM in fermentation on a commercial scale, and yields in sugar medium comparable to those obtained by the conventional method. It was confirmed that it was a raw material capable of producing glumic acid while maintaining the concentration of glucumic acid.

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Abstract

L'invention se rapporte à un procédé de fabrication de diverses matières sucrées, employé dans la fermentation effectuée à partir de différentes substances à base d'amidon et permettant de réduire au minimum la quantité d'eau utilisée, ce qui rend le procédé sensiblement exempt d'eaux ou de matières usées. Les substances à base d'amidon sont broyées et divisées en une fraction légère supérieure et une fraction lourde inférieure par des opérations de séparation telles que la flottation sous pression. La fraction inférieure est ensuite broyée de façon répétitive et séparée, alors que les matières sucrées destinées à la fermentation sont obtenues par l'hydrolyse de la fraction inférieure finalement séparée. Les fractions séparées supérieures peuvent être utilisées en tant qu'aliments ou engrais. Les filtrats et les surnageants formés lors des opérations de séparation sont réintroduits immédiatement avant les étapes de séparation ou de broyage et réutilisés.
PCT/JP1998/001554 1998-04-03 1998-04-03 Procede de fabrication de matieres sucrees destinees a la fermentation WO1999051782A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
PCT/JP1998/001554 WO1999051782A1 (fr) 1998-04-03 1998-04-03 Procede de fabrication de matieres sucrees destinees a la fermentation
CN98806718A CN1099466C (zh) 1998-04-03 1998-04-03 发酵用粗糖原料的生产方法
BRPI9809714-8A BR9809714B1 (pt) 1998-04-03 1998-04-03 processo para produzir um material de açúcar bruto para fermentação.
MYPI99001279A MY129273A (en) 1998-04-03 1999-04-02 Method for producing raw sugar material for fermentation

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/JP1998/001554 WO1999051782A1 (fr) 1998-04-03 1998-04-03 Procede de fabrication de matieres sucrees destinees a la fermentation

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WO1999051782A1 true WO1999051782A1 (fr) 1999-10-14

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2001309751A (ja) * 2000-05-02 2001-11-06 Ajinomoto Co Inc 飼料用添加物
WO2008090707A1 (fr) * 2007-01-25 2008-07-31 Japan International Research Center For Agricultural Sciences Méthode de production d'éthanol ou d'acide lactique

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS57152888A (en) * 1981-03-14 1982-09-21 Mitsui Eng & Shipbuild Co Ltd Alcoholic fermentation of raw potato by enzymatic process
JPS57186494A (en) * 1981-05-07 1982-11-16 Suntory Ltd Fermentation of alcohol
JPH06502547A (ja) * 1991-07-03 1994-03-24 ビオディヌ　ブルゴーニュ 部分的に加水分解された澱粉を連続的に生産する方法、この方法によって得られる製品およびその応用

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS57152888A (en) * 1981-03-14 1982-09-21 Mitsui Eng & Shipbuild Co Ltd Alcoholic fermentation of raw potato by enzymatic process
JPS57186494A (en) * 1981-05-07 1982-11-16 Suntory Ltd Fermentation of alcohol
JPH06502547A (ja) * 1991-07-03 1994-03-24 ビオディヌ　ブルゴーニュ 部分的に加水分解された澱粉を連続的に生産する方法、この方法によって得られる製品およびその応用

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2001309751A (ja) * 2000-05-02 2001-11-06 Ajinomoto Co Inc 飼料用添加物
WO2008090707A1 (fr) * 2007-01-25 2008-07-31 Japan International Research Center For Agricultural Sciences Méthode de production d'éthanol ou d'acide lactique

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BR9809714A (pt) 2000-07-11
CN1099466C (zh) 2003-01-22
MY129273A (en) 2007-03-30
BR9809714B1 (pt) 2011-01-11
CN1261921A (zh) 2000-08-02

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