WO2015007568A1 - Verfahren zur trocknung von biomasse - Google Patents

Verfahren zur trocknung von biomasse Download PDF

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Publication number
WO2015007568A1
WO2015007568A1 PCT/EP2014/064569 EP2014064569W WO2015007568A1 WO 2015007568 A1 WO2015007568 A1 WO 2015007568A1 EP 2014064569 W EP2014064569 W EP 2014064569W WO 2015007568 A1 WO2015007568 A1 WO 2015007568A1
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WO
WIPO (PCT)
Prior art keywords
biomass
drying
cells
particulate
weight
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/EP2014/064569
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German (de)
English (en)
French (fr)
Inventor
Nicolas Rudinger
Christian Rabe
Wilfried BLÜMKE
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Evonik Industries AG
Original Assignee
Evonik Industries AG
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 Evonik Industries AG filed Critical Evonik Industries AG
Priority to DK14736808.8T priority Critical patent/DK3021683T3/en
Priority to CN201480040627.8A priority patent/CN105530821A/zh
Priority to BR112016000918-5A priority patent/BR112016000918B1/pt
Priority to US14/904,665 priority patent/US10531679B2/en
Priority to EP14736808.8A priority patent/EP3021683B1/de
Publication of WO2015007568A1 publication Critical patent/WO2015007568A1/de
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K10/00—Animal feeding-stuffs
    • A23K10/10—Animal feeding-stuffs obtained by microbiological or biochemical processes
    • A23K10/12—Animal feeding-stuffs obtained by microbiological or biochemical processes by fermentation of natural products, e.g. of vegetable material, animal waste material or biomass
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23B—PRESERVATION OF FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES; CHEMICAL RIPENING OF FRUIT OR VEGETABLES
    • A23B2/00—Preservation of foods or foodstuffs, in general
    • A23B2/90—Preservation of foods or foodstuffs, in general by drying or kilning; Subsequent reconstitution
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23B—PRESERVATION OF FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES; CHEMICAL RIPENING OF FRUIT OR VEGETABLES
    • A23B2/00—Preservation of foods or foodstuffs, in general
    • A23B2/90—Preservation of foods or foodstuffs, in general by drying or kilning; Subsequent reconstitution
    • A23B2/95—Fluidised-bed drying
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/008—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from microorganisms
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/009—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from unicellular algae
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/18—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from yeasts
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J3/00—Working-up of proteins for foodstuffs
    • A23J3/20—Proteins from microorganisms or unicellular algae
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J3/00—Working-up of proteins for foodstuffs
    • A23J3/30—Working-up of proteins for foodstuffs by hydrolysis
    • A23J3/32—Working-up of proteins for foodstuffs by hydrolysis using chemical agents
    • A23J3/34—Working-up of proteins for foodstuffs by hydrolysis using chemical agents using enzymes
    • A23J3/347—Working-up of proteins for foodstuffs by hydrolysis using chemical agents using enzymes of proteins from microorganisms or unicellular algae
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K10/00—Animal feeding-stuffs
    • A23K10/10—Animal feeding-stuffs obtained by microbiological or biochemical processes
    • A23K10/16—Addition of microorganisms or extracts thereof, e.g. single-cell proteins, to feeding-stuff compositions
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K10/00—Animal feeding-stuffs
    • A23K10/10—Animal feeding-stuffs obtained by microbiological or biochemical processes
    • A23K10/16—Addition of microorganisms or extracts thereof, e.g. single-cell proteins, to feeding-stuff compositions
    • A23K10/18—Addition of microorganisms or extracts thereof, e.g. single-cell proteins, to feeding-stuff compositions of live microorganisms
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K20/00—Accessory food factors for animal feeding-stuffs
    • A23K20/10—Organic substances
    • A23K20/158—Fatty acids; Fats; Products containing oils or fats
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K30/00—Processes specially adapted for preservation of materials in order to produce animal feeding-stuffs
    • A23K30/20—Dehydration
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K40/00—Shaping or working-up of animal feeding-stuffs
    • A23K40/10—Shaping or working-up of animal feeding-stuffs by agglomeration; by granulation, e.g. making powders
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K50/00—Feeding-stuffs specially adapted for particular animals
    • A23K50/80—Feeding-stuffs specially adapted for particular animals for aquatic animals, e.g. fish, crustaceans or molluscs
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N1/00—Microorganisms; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
    • C12N1/12—Unicellular algae; Culture media therefor
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2250/00—Food ingredients
    • A23V2250/18—Lipids
    • A23V2250/186—Fatty acids
    • A23V2250/1882—Polyunsaturated fatty acids
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2250/00—Food ingredients
    • A23V2250/20—Natural extracts
    • A23V2250/202—Algae extracts
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2300/00—Processes
    • A23V2300/10—Drying, dehydrating
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2300/00—Processes
    • A23V2300/14—Extraction

Definitions

  • the present invention relates to a method for the gentle drying of a biomass, in particular a biomass containing an oxidation-sensitive valuable material, as well as the biomass obtained by this method.
  • microbial cells for the production of valuable substances.
  • An example of such recyclables are food components, especially lipids such as polyunsaturated fatty acids.
  • lipids such as polyunsaturated fatty acids.
  • other fungi and algae play a special role in the production of such valuable substances.
  • omega-3 fatty acids Certain valuable substances, in particular polyunsaturated fatty acids (PUFAs), are an important component of human and animal nutrition.
  • the source of omega-3 fatty acids was first and foremost fish. Later, it was discovered that certain microbes produce heterotrophic omega-3 fatty acids in large quantities, whereby fatty acid production can be favorably influenced by the choice of specific reaction parameters.
  • the omega-3 fatty acids can then be extracted from the cells or the cells can be used directly in feed or food in the form of biomass.
  • the object of the invention is achieved by a method for drying a biomass containing an oxidation-sensitive valuable material, characterized in that the method comprises a drying step in which gas is passed over the biomass in cycle gas mode.
  • “Circulating gas mode” means that the gas used for drying is circulated over the biomass.
  • the process step which consists in the transfer of gas in the gas cycle over the biomass is preferably a thermal process, ie the gas used is preferably a temperature above the saturation temperature of the solvent to be evaporated.
  • the gas used is preferably air with a reduced content of oxygen.
  • the gas conducted in the cycle gas mode preferably has an oxygen content of less than 20% by weight, preferably less than 15% by weight, in particular from 5 to 13% by weight.
  • the gas is preferably generated by passing the air over a burner and heating it in this way. At the same time, this reduces the oxygen content of the air to less than 20% by weight, preferably less than 15% by weight, in particular from 5 to 13% by weight.
  • the gas is always readjusted in the same way to a constant
  • the drying is preferably in a
  • Fluidized bed process performed.
  • the biomass is converted directly into a granulate, so that it is a
  • Spray granulation is.
  • biomass contained in the fermentation broth can be dried and granulated in one step and thus only one process step from the biomass-containing fermentation broth to the finished product is required.
  • Another advantage of this method is that the fluidized bed process can be operated continuously and stationary: biomass-containing
  • Fermentation broth can be sprayed continuously and the finished product can be discharged continuously.
  • the fluidized bed in this case preferably has one in the process according to the invention
  • Fluidized bed process for example, a fluidized bed granulation can be performed.
  • this usually requires the biomass-containing
  • Fluidized bed plants which can be used in processes according to the invention are available, for example, from Glatt GmbH (Germany).
  • the biomass to be used according to the invention comprises cells, but may additionally comprise further constituents.
  • the biomass is preferably the product of a fermentative cultivation process.
  • the biomass may in particular also contain constituents of the fermentation medium. These ingredients may be, in particular, salts, antifoaming agents and unreacted carbon source and / or nitrogen source.
  • the cell content in this biomass is preferably at least 70% by weight, preferably at least 75% by weight.
  • the cell content in the biomass may, if appropriate, be increased to at least 80 or at least 90% by weight prior to carrying out the drying by means of appropriate washing steps.
  • the biomass obtained in the fermentation process can also be used directly in the drying process.
  • the cells contained in the biomass can be cells that already naturally produce valuable substances, preferably lipids, in particular PUFAs, but it can also be cells that are produced by appropriate genetic engineering
  • lipids in particular PUFAs.
  • the production can be autotrophic, mixotrophic or heterotrophic.
  • the biomass preferably comprises cells which produce lipids, in particular PUFAs, heterotrophically.
  • the cells are preferably algae, fungi, in particular yeasts, or protists, but cells of oil-producing plants, for example, are also suitable. Particularly preferred are cells of microbial algae or fungi.
  • the cells of oil-producing plants are, in particular, the seeds of soya, flax, oilseed rape, maize, cotton, thistle and sunflower.
  • Yeasts of Yarrowia, Candida, Rhodotorula, Rhodosporidium, Cryptococcus, Trichosporon and Lipomyces are particularly suitable as cells of oil-producing yeasts.
  • the biomass preferably comprises cells of the taxon
  • Labyrinthulomycetes (labyrinthulea, slime, mucus), especially those of the family Thraustochytriaceae.
  • the family of Thraustochytriaceae includes the genera Althomia, Aplanochytrium, Elnia, Japonochytrium, Schizochytrium,
  • the biomass particularly preferably comprises cells of the genera Thraustochytrium or Schizochytrium, especially those of the genus
  • schizochytrium also encompasses the new genera which has recently been produced by reclassification of the genus Schizochytrium
  • Aurantiochytrium limacinum in particular the strain Schizochytrium limacinum SR21.
  • the oxidation-sensitive valuable substance is preferably a
  • oxidation-sensitive lipid in particular an unsaturated fatty acid, more preferably a polyunsaturated fatty acid (PUFA) or highly unsaturated fatty acid (HUFA).
  • unsaturated fatty acid more preferably a polyunsaturated fatty acid (PUFA) or highly unsaturated fatty acid (HUFA).
  • PUFA polyunsaturated fatty acid
  • HUFA highly unsaturated fatty acid
  • the cells contained in the biomass are preferably characterized by having a valuable substance content, preferably lipid content, particularly preferably PUFA content, of at least 20% by weight, preferably at least 30% by weight, in particular at least 40% by weight .-%, in each case based on the cell dry matter, have.
  • a valuable substance content preferably lipid content, particularly preferably PUFA content
  • lipids are present in the form of triglycerides, preferably at least 50% by weight, in particular at least 75% by weight and in a particularly preferred embodiment at least 90% by weight of the lipids contained in the cell in the form of triglycerides.
  • the lipids contained in the cell preferably comprise polyunsaturated fatty acids (PUFAs), with preferably at least 10% by weight, in particular at least 20% by weight, particularly preferably from 20 to 60% by weight, in particular from 20 to 40% by weight.
  • the fatty acids contained in the cell constitute PUFAs.
  • polyunsaturated fatty acids (PUFAs) are fatty acids which have at least two, in particular at least three, C-C double bonds.
  • highly unsaturated fatty acids are preferred.
  • HUFAs are fatty acids which have at least four C-C double bonds.
  • the PUFAs can be present in the cell in free form or in bound form. Examples of the presence in bound form are phospholipids and esters of PUFAs,
  • a majority of PUFAs is in the form of triglycerides, preferably at least 50 wt .-%, in particular at least 75 wt .-% and in a particularly preferred embodiment, at least 90 wt .-% of the PUFAs contained in the cell in the form of triglycerides available.
  • Preferred PUFAs are omega-3 fatty acids and omega-6 fatty acids, omega-3 fatty acids being particularly preferred.
  • Preferred omega-3 fatty acids hereby comprise eicosapentaenoic acid (EPA, 20: 5 ⁇ -3), in particular the (5Z, 8Z, 11Z, 14Z, 17Z) -ecoso-5,8,11,14,17-pentaenoic acid , and the docosahexaenoic acid (DHA, 22: 6 ⁇ -3), in particular the (4Z, 7Z, 10Z, 13Z, 16Z, 19Z) docosa-4,7,10,13,16,19-hexaenoic acid, with docosahexaenoic acid being particularly preferred.
  • EPA eicosapentaenoic acid
  • DHA docosahexaenoic acid
  • a method for producing the biomass, in particular such biomass, which comprises lipids, in particular PUFAs, containing cells, in particular the order Thraustochytriales, are described in detail in the prior art.
  • the preparation is usually carried out by culturing cells in the presence of a carbon source and a nitrogen source in a fermenter.
  • biomass densities of more than 100 grams per liter and production rates of more than 0.5 grams of lipid per liter per hour can be achieved (WO 01/54510).
  • the process is preferably carried out as a so-called fed-batch process, i. that the carbon and nitrogen sources are supplied incrementally during the fermentation.
  • the lipid production can be induced after reaching the desired biomass by different measures,
  • the fermentation of the cells is preferably carried out in a medium of low salinity, especially to prevent corrosion. This can be achieved in that, instead of sodium chloride, chlorine-free sodium salts, such as, for example, sodium sulfate,
  • Chloride is preferably used in amounts of less than 3 g / l, in particular less than 500 mg / l, particularly preferably less than 100 mg / l, in the fermentation.
  • the source of carbon is both alcoholic and non-alcoholic
  • alcoholic carbon sources are methanol, ethanol and isopropanol.
  • non-alcoholic carbon sources are fructose, glucose, sucrose, molasses, starch and corn syrup.
  • Suitable sources of nitrogen include both inorganic and organic nitrogen sources.
  • inorganic nitrogen sources are nitrates and ammonium salts, especially ammonium sulfate and ammonium hydroxide.
  • organic nitrogen sources are nitrates and ammonium salts, especially ammonium sulfate and ammonium hydroxide.
  • Nitrogen sources are amino acids, especially glutamate, and urea.
  • inorganic or organic phosphorus compounds and / or known growth stimulants such as yeast extract or corn steep liquor, may also be added to positively affect the fermentation.
  • the fermentation of the cells is preferably carried out at a pH of 5 to 1 1, in particular 6 to 10, and preferably at a temperature of at least 20 ° C, in particular 20 to 40 ° C, particularly preferably at least 30 ° C.
  • Fermentation process takes up to about 100 hours. After completion of the fermentation, the biomass is harvested. Preferably, after harvesting the biomass, or possibly even shortly before harvesting the biomass, pasteurization of the cells occurs to kill the cells and to inactivate enzymes that might promote the breakdown of the lipids. The pasteurization takes place
  • the biomass preferably by heating the biomass to a temperature of 50 to 121 ° C for a period of 5 to 60 minutes.
  • antioxidants are BHT, BHA, TBHA, ethoxyquin, beta-carotene, vitamin E and vitamin C.
  • the antioxidant if used, is preferably added in an amount of from 0.01 to 2% by weight.
  • a part of the fermentation medium can now be separated from the biomass and thus the solids content can be increased.
  • This can be done in particular by centrifugation, filtration, in particular ultrafiltration or microfiltration, decantation and / or solvent evaporation.
  • the solvent evaporation is preferably carried out using a rotary evaporator, a thin film evaporator or a falling film evaporator in a single-stage or multi-stage process.
  • solvent evaporation for example, the reverse osmosis for the purpose of narrowing the fermentation broth into consideration.
  • step is preferably carried out a concentration of the fermentation medium to a solids content of
  • the biomass to be dried in a method according to the invention is preferably in the form of a suspension with the previously stated solids content, wherein it is at the liquid component of the suspension is preferably fermentation broth or concentrated fermentation broth.
  • the biomass can also be dried directly after harvest by a cycle gas process, especially if the fermentation broth obtained already has a high solids content, preferably as stated above.
  • Oxygen concentration is preferably reduced as indicated above.
  • the drying of the biomass according to the invention is preferably carried out in a fluidized bed granulation process.
  • the biomass-containing fermentation broth is sprayed for this purpose in the fluidized bed Trocknungsgranulationsstrom.
  • Dry granulation plant is shown schematically in Fig. 1 of EP 0809940.
  • the drying gas is introduced from below.
  • the majority of the moisture of the sprayed fermentation broth evaporates and the resulting granules are held in suspension by the gas flow of the drying gas.
  • the particles are separated from each other and so freely accessible when spraying additional liquid in the bed for the spray drops.
  • Product particles of the desired size are withdrawn continuously in a classifying flue from the fluidized bed.
  • the fluidized bed or the bed of particles which must be present at the beginning of the fluidized bed granulation drying, preferably consists of dried particles of the biomass used for drying, for example from a batch of a previous run. However, it is just as possible to use a material other than fluidized bed to initiate fluidized bed granulation drying.
  • a particular advantage of the fluidized bed granulation process is that the process can be operated continuously and in one step, the biomass-containing
  • Fermentation broth can be converted into a product with the desired particle size.
  • the particles produced also have excellent strength and have due to their substantially round shape due to very good bulk and flow properties.
  • the particles also have a low residual moisture content.
  • drying according to the invention is preferably a free-flowing, finely divided or coarse-grained product, preferably granules obtained.
  • a product having the desired grain size can be obtained from the granules obtained by sieving or dust separation.
  • a free-flowing finely divided powder has been obtained, this can optionally be converted by suitable compacting or granulation processes into a coarse-grained, free-flowing, storable and substantially dust-free product.
  • f one-part is meant according to the invention a powder with a predominant proportion (> 50%) of a particle size of 20 to 500 micrometers in diameter.
  • Dust-free is to be understood according to the invention as a powder which contains only small amounts ( ⁇ 5%) of particle sizes below 100 micrometers.
  • the determination of the grain or particle sizes is carried out according to the invention preferably by methods of laser diffraction spectrometry.
  • the methods to be used are described in the textbook “Particle Size Measurement in Laboratory Practice” by RH Müller and R. Schuhmann, Stuttgart (1996) and in the textbook “Introduction to Particle Technology” by M. Rhodes, Verlag Wiley & Sons (1998). If different methods are applicable, preference is given to the first applicable methodology from the textbook of RH Müller and R. Schuhmann
  • the products obtained according to the invention preferably have a content of at least 80% by weight, in particular at least 90% by weight, more preferably at least 95% by weight, especially at least 97% by weight, of particles having a particle size of from 100 to 3500 micrometers, preferably 1000 to 3000 micrometers, especially 1500 to 2500 micrometers.
  • Due to the production process are preferably at least 50 wt .-%, in particular at least 70 wt .-%, particularly preferably at least 90 wt .-%, especially in
  • Substantial spherical formation of the particles causes the excellent bulk and flow properties of the product according to the invention.
  • the term "essentially spherical” means that the diameter of a particle is substantially the same in all spatial directions. “Substantially equal” means that the deviation of the diameter of a particle in any two spatial directions is at most 20%. , preferably not more than 15%, in particular not more than 10%, particularly preferably not more than 5%.
  • the proportion of dust i. Particles having a particle size of less than 100 micrometers, is preferably at most 1 wt .-%, more preferably at most 0.5 wt .-%.
  • the bulk density of the products according to the invention is preferably 400 to 800 kg / m 3, more preferably 450 to 700 kg / m 3.
  • the present invention thus also relates to a particulate biomass obtainable by a process according to the invention and to a particulate biomass which contains an oxidation-sensitive valuable substance having the abovementioned properties, in particular having the properties mentioned above with regard to particle size and Particle distribution.
  • a particulate biomass obtainable by a process according to the invention and to a particulate biomass which contains an oxidation-sensitive valuable substance having the abovementioned properties, in particular having the properties mentioned above with regard to particle size and Particle distribution.
  • the biomass obtained according to the invention can be used in different ways. After drying the biomass according to the invention, storage or packaging of the dried biomass is preferably carried out. Subsequently, the biomass can be used, for example, to produce a feed or food or to isolate the valuable material from the biomass.
  • a feed or food containing a particulate biomass according to the invention is a further subject of the present invention.
  • a further subject of the present invention is therefore also a process for isolating the valuable substance from a particulate composition according to the invention.
  • the particulate biomass is preferably subjected to a cell disruption process.
  • the isolation of the valuable material can alternatively also be carried out directly from the particulate biomass, without unlocking it beforehand.
  • the dried biomass Before carrying out the cell disruption process, it is preferable to prepare a cell suspension based on the dried biomass.
  • the dried biomass For this purpose, the dried
  • the cell digestion can then be carried out using those known to the person skilled in the art
  • Cell disruption procedures such as by a screw extruder, a beater mill, an air jet mill, or by application of elevated pressure,
  • the cell digestion can be carried out by the use of cell-wall-digesting enzymes.
  • the cell digestion is preferably carried out according to the invention using a rotor-stator system.
  • the rotor-stator system is based on a stationary part called a stator and a rotating part, the rotor.
  • the rotor typically has a peripheral speed of at least 5 m / s, for example 10 to 30 m / s, the gap width between rotor and stator can be, for example 0.1 - 0.5 mm.
  • the suspension is produced in the rotor-stator system using a solids mixing attachment.
  • a solids mixing attachment is to be understood as meaning a device which permits the separate introduction of on the one hand solid and on the other hand water or aqueous solution into the rotor-stator system. The suspension is thus produced only during the cell disruption or immediately before the cell digestion by mixing in the solids-mixing attachment.
  • suspensions with very high solids contents can be subjected to cell disruption using such a solids-mixing attachment, which is particularly advantageous with regard to the subsequent processing.
  • Suspensions used in the rotor-stator system using a solids mixing attachment preferably have a solids content of 20-50% by weight, more preferably 30-50% by weight.
  • an aqueous solution may in particular contain other food components, such as vitamins or salts.
  • the energy input to the cells, in particular using a rotor-stator system, according to the invention is preferably at most 50 kWh per ton of suspension, in particular not more than 40, 35 or 30 kWh per ton of suspension, particularly preferably not more than 25, 20 or 15 kWh per ton of suspension , Preferred ranges here are energy inputs of 0.1-50 kWh per ton of suspension, in particular 0.3-45 kWh, particularly preferably 0.5-40 kWh, in particular 0.8-35 kWh, especially 1-30 kWh, in particular 1 , 5 - 25 kWh, 2 - 20 kWh or 3 - 15 kWh, each per ton of suspension.
  • the "cell disintegration rate" of the method according to the invention is preferably at least 50%, more preferably at least 60, 70 or 80%, especially at least 85, 90 or 95% to understand the total number of cells.
  • the cell digestion rate may be visually using a Microscopes are determined as the ratio of the number of disrupted cells in relation to the total number of cells.
  • antioxidants may additionally be present in the cell suspension used for cell disruption.
  • Preferred antioxidants are BHT, BHA, TBHA, ethoxyquin, beta-carotene, vitamin E and vitamin C.
  • the antioxidant if used, is preferably present in an amount of from 0.01 to 2% by weight.
  • the antioxidants are added to the fermentation medium after completion of the fermentation.
  • the isolation of the valuable material from the biomass can be carried out both from the intact dried biomass and from the digested biomass.
  • a simple mechanical separation of the cell debris can be carried out, for example by decantation, filtration or centrifugation.
  • the isolation of the valuable material can otherwise be carried out both from the intact and from the digested biomass, for example by solvent extraction.
  • the solvent can be correspondingly removed again after the removal of the valuable substance, for example by applying a reduced pressure.
  • the isolation of the valuable substance can be carried out, for example, by supercritical liquid extraction.
  • the solvents which can be used are the solvents known to the person skilled in the art, for example chloroform, ether, hexane, methylene chloride or methanol.
  • the separation of the oil can also be effected, for example, by using another oil for the extraction of the oil according to the invention.
  • the oil may then undergo a chemical or physical refining.
  • Refining can be degumming, bleaching, filtering, etc.
  • Deodorizing and / or polishing the crude include. Subsequently, if necessary, individual oil components can be isolated.
  • Both the intact and the digested biomass and the recyclables isolated from the biomass can be used for the production of a food or feed in which the biomass or the valuable material is preferably mixed with other foodstuffs. or feed ingredients and then processed into the food or feed.
  • Extrusion process to obtain ready-to-eat portions of the food or feed.
  • a pelleting process can also be used.
  • a screw or twin-screw extruder is preferably used.
  • the extrusion process is preferably carried out at a temperature of 80 - 220 ° C, especially 100 - 190 ° C, a pressure of 10 - 40 bar, and a
  • the residence time of the introduced mixture is preferably 5 to 30 seconds, in particular 10 to 20 seconds.
  • this comprises
  • a compaction and a compression step Before carrying out the extrusion process, the components are preferably intimately mixed. This is preferably done in a drum equipped with blades. In this mixing step, in a preferred embodiment, a steam injection takes place, in particular in order to effect the swelling of the preferably contained starch.
  • the other food or feed ingredients are preferably comminuted before mixing with the digested cells, if necessary
  • a preferred method for producing a food or feed according to the invention therefore comprises the following steps: a) production of a biomass, preferably by fermentation of fungi or microalgae, which produce a valuable substance, preferably a lipid, more preferably omega-3 fatty acids; b) gentle drying of the resulting biomass, wherein the gentle drying comprises the passing of gas in the cycle gas method and wherein the oxygen content of the gas is preferably less than 20 wt .-%, in particular less than 15 wt .-%, particularly preferably 5 to 13 wt .-%, and is preferably used for drying the Sprühgranulationshabilit previously described; c) mixing the biomass and / or recyclables isolated therefrom, if appropriate after previously carrying out a cell disruption process, with other food or feed ingredients; d) Preparation of the final product by a comp
  • Food or feed comprises the following steps: a) production of a biomass, preferably by fermentation of fungi or
  • Microalgae especially of slime fungi, which produce a valuable substance, preferably a lipid, more preferably omega-3 fatty acids; b) gentle drying of the resulting biomass to a moisture content of preferably less than 15 wt .-%, preferably less than 10 wt .-%, in particular 1-9 wt .-%, more preferably less than 5 wt .-%, in particular 1 - 4.5 wt .-%, wherein the gentle drying comprises the passing of gas in the cycle gas mode of operation and wherein the oxygen content of the gas in this case preferably less than 20 wt .-%, in particular less than 15 wt .-%, particularly preferably 5 bis 13 wt .-%, and is preferably used for drying the previously described Sprühgranulationshabilit; c) transfer of the biomass into a cell suspension having a moisture content of at least 30 wt .-%, preferably 30 to 90 wt .-%, particularly preferably 40 to 80
  • Preferred methods according to the invention for the production of a foodstuff or feedstuff are preferably characterized in that no higher energy input to the biomass takes place in any process step than 50 kWh per tonne of suspension.
  • the energy input to the biomass is preferably not more than 40 or 35 kWh, in particular not more than 30 or 25 kWh, particularly preferably 20 or 15 kWh, in each case per ton
  • the digested cells preferably make up 0.5-20% by weight, in particular 1-10% by weight, preferably 2-8% by weight, of the foodstuff or feed
  • the food or feed is preferably an aquaculture agent or food or feed for use in poultry, pig breeding or cattle breeding.
  • the feed may also be a feed used to breed micro-organisms that can be used as feed in aquaculture.
  • the microorganisms may be, for example, nematodes, crustaceans or rotifers.
  • the feed is preferably flaked, spherical or tablet-shaped. An available by extrusion
  • Feed preferably has a moisture content of less than 5% by weight, more preferably from 0.2 to 4% by weight.
  • the other food or feed ingredients are preferably selected from proteinaceous, carbohydrate-containing, nucleic acid-containing and lipid-soluble components and optionally other fatty components and further from other additives such as minerals, vitamins, pigments and amino acids.
  • structuring substances may also be present in order to improve the texture or the appearance of the feedstuff.
  • binders can be used to influence the consistency of the feed.
  • a preferred component that is both a nutrient and a structurant is starch.
  • a protein-containing component which additionally contains fats, can be used, for example, fish meal, krill flour, shellfish, squid or Schrimpsschalen.
  • fish oil can be used as a fat-containing component.
  • a fat-containing component can also be used a vegetable oil, in particular oil from soybeans, rapeseeds, sunflower seeds and flaxseed.
  • carbohydrate-containing component for example, wheat flour, sunflower flour, soybean meal or
  • Grain gluten can be used.
  • the total content of oil in the feed - including the oil from the oil-containing cells - is preferably 15-50 wt .-%.
  • the feed for use in aquaculture is preferably used to
  • fin fish and crustaceans which are preferably used to nourish humans. These include in particular carp, tilapia, catfish, tuna, salmon, trout, baramundi, bream, perch, cod, shrimp, lobster, crab, shrimp and crayfish. Particularly preferred is a feed for salmon farming.
  • the most popular salmon species are Atlantic salmon, red salmon, masu salmon, king salmon, keta salmon, silver salmon, Danube salmon, pacific salmon and pink salmon.
  • fish meal or fish oil thus obtained can in turn be used in aquaculture for the breeding of food fish or crustaceans.
  • the aquaculture can take place in ponds, tanks, basins or even in delimited areas in the sea or in lakes, in particular in cages or net pens. Aquaculture can be used to grow the ready-made food fish, but can also be used to raise juvenile fish, which are then released to feed the fish
  • a further subject of the present invention is accordingly also a method for breeding animals, in particular fin fish or crustaceans, preferably salmon, in which a feed according to the invention is used.
  • a further subject of the present invention is furthermore an animal, in particular a finfish or shellfish, obtainable by such a method according to the invention.
  • the present invention furthermore relates to processes for obtaining an oxidation-sensitive valuable substance from a biomass comprising a drying step according to the invention.

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DK14736808.8T DK3021683T3 (en) 2013-07-16 2014-07-08 METHOD OF DRYING BIOMASS
CN201480040627.8A CN105530821A (zh) 2013-07-16 2014-07-08 干燥生物质的方法
BR112016000918-5A BR112016000918B1 (pt) 2013-07-16 2014-07-08 Método para secagem de biomassa
US14/904,665 US10531679B2 (en) 2013-07-16 2014-07-08 Method for drying biomass
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CL2016000098A1 (es) 2016-08-12
EP3021683A1 (de) 2016-05-25
US20160183565A1 (en) 2016-06-30
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CN105530821A (zh) 2016-04-27
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