EP3200611A1

EP3200611A1 - Method for producing a granular biomass which contains an oxidation-sensitive valuable substance

Info

Publication number: EP3200611A1
Application number: EP15766527.4A
Authority: EP
Inventors: Christian Rabe; Mathias DERNEDDE; Alexander SCHRICKEL; Horst Priefert; Stefan Eils; Michael Diehl
Original assignee: Evonik Degussa GmbH
Current assignee: Evonik Operations GmbH
Priority date: 2014-10-02
Filing date: 2015-09-22
Publication date: 2017-08-09
Also published as: DK201770205A1; CL2017000753A1; WO2016050560A1; BR112017006835A2; DK180022B1; CA2958464A1; CN106793802A; US20170298318A1

Abstract

According to the invention, a particulate biomass which contains an oxidation-sensitive valuable substance is transformed into an especially easy-to-use product when it is granulated while adding an agglomeration aid.

Description

Process for producing a granulated biomass containing a

contains oxidation-sensitive recyclable material

The present invention relates to a process for the production of a granulated biomass containing an oxidation-sensitive valuable substance, as well as the granulated biomass obtainable by this process.

The importance of microbial cells for the production of valuable substances is known to the person skilled in the art. An example of such recyclables are food components, especially lipids such as polyunsaturated fatty acids. In addition to bacteria and yeasts, other fungi and algae play a special role in the production of such valuable substances.

Certain valuable substances, in particular polyunsaturated fatty acids (PUFAs), are an important component of the diet of humans and animals. The source of PUFAs was first and foremost fish. Furthermore, it is known that certain microbes produce heterotrophic PUFAs in large quantities, whereby the fatty acid production can be favorably influenced by the choice of specific reaction parameters. The PUFAs can then be obtained from the cells or the cells can be used in the form of biomass directly in feed or food.

To prepare the biomass for use in feed or food, it is necessary to convert them into a manageable, flowable form. However, it has been found that the processing of the biomass described in the prior art often leads to a poorly handled, non-flowable, generally hygroscopic product. This is especially the case when the biomass contains a high proportion of lipids, especially triglycerides.

Spray drying of the biomass often produces a dusty and also poorly flowable product.

It was therefore an object of the present invention to provide a process which permits the transfer of the particulate biomass into a more easily handled, flowable, dust-free and, if possible, non-hygroscopic defined particulate product. In the workup, in particular, the contained valuable material should remain largely intact. In this respect, the workup should in particular also ensure that the cell membranes of the cells contained in the biomass are largely retained intact in order to prevent the oxidative degradation of the contained valuable material. Furthermore, it should preferably also be prevented as far as possible that possibly freed valuable material, for example by oxidative degradation, is damaged.

According to the invention, it has been found that the object according to the invention can be achieved by using a particulate starting biomass using a

Granulation agent is granulated. This procedure leads to a clearly defined, very easy to handle, flowable, dust-free and non-hygroscopic product, which is very well suited for incorporation in feed or foodstuffs.

A first subject of the present invention is therefore a process for producing a particulate biomass containing an oxidation-sensitive valuable material, characterized in that a particulate starting biomass using a

Granulation or granulation is subjected to granulation.

The term "granulation" or "granulation" according to the invention means the transfer of a finely divided particulate powder into a coarser particulate powder, the coarse-grained powder obtainable preferably having a particle size of 0.1 to 2.0 mm (d50) and preferably a good one Has flowability.

The present invention thus also relates to a particulate biomass obtainable by a process according to the invention.

Another object of the present invention is therefore also a particulate biomass containing an oxidation-sensitive valuable material, characterized in that the particulate biomass contains an agglomeration aid.

The agglomeration aid to be used according to the invention is preferably selected from optionally modified carbohydrates, proteins, further organic

Polymers, inorganic substances and mixtures thereof. As optionally modified carbohydrates, it is possible, for example, to use monomeric or oligomeric sugars and mixtures thereof, in particular glucose, sucrose or maltodextrins. Preferably, the optionally modified carbohydrate is an optionally modified polysaccharide, wherein as agglomeration aids preferably guar gum, gum arabic, guar gum, locust bean gum, xanthan gum, agar, carrageenan, starch, in particular corn starch, tapioca starch or potato starch, cellulose or their Derivatives, hemicellulose or their derivatives, alginic acid or maltodextrin, and mixtures thereof.

Among "derivatives" of carbohydrates and "modified" carbohydrates are

According to the invention in particular by alkyl, especially Ci-6-alkyl, especially Ci-4-alkyl, by carboxyalkyl, especially carboxy-Ci-6-alkyl, especially carboxy-Ci-4-alkyl-, and by Hydroxyalkyl, especially hydroxy-Ci-6-alkyl, especially hydroxy-Ci-4-alkyl groups modified carbohydrates to understand.

Particular preference is given to using cellulose modified as an agglomeration aid, in particular by carboxy-modified cellulose, in particular carboxymethyl cellulose and / or hydroxypropylmethyl cellulose, very particularly preferably

Carboxymethyl cellulose. The preferably used sodium salt of carboxymethyl cellulose is obtainable, for example, by reaction of sodium chloroacetate with

Alkali cellulose and commercially available under the trade name Blanose (Ashland, USA).

Modified celluloses which can be used according to the invention, in particular carboxymethyl celluloses, preferably have an average molecular weight of 80,000 to 800,000 g / mol, in particular 90,000 to 700,000 g / mol, particularly preferably 100,000 to 600,000 g / mol, in particular 150,000 to 400,000 g / mol, especially 200,000 to 300,000 g / mol.

Likewise particularly preferred maltodextrins are used as agglomeration aids. Maltodextrins are water-soluble carbohydrate mixtures obtainable by hydrolysis of starch. They are a mixture of monomers, dimers, oligomers and polymers of glucose. Depending on the degree of hydrolysis, the percentage composition differs. The degree of hydrolysis is given in dextrose equivalents (DE). Starch has a DE value of 1, glucose has a DE value of 100.

Maltodextrins have a DE value of 3 to 20. According to the invention, maltodextrins be used with any DE values, but preferably a maltodextrin is used with a DE value of 3 to 10.

Furthermore, proteins can be used as agglomeration aids, in particular casein, gelatin, collagen, wheat gluten and mixtures thereof. Furthermore, organic polymers can be used as agglomeration aids, in particular lignosulfonates, polymethylolcarbamides, polyacrylic acids or

Polyvinyl alcohols and mixtures thereof.

Furthermore, inorganic substances can be used as agglomeration aids, in particular silicates, preferably bentonites, hexametaphosphate and

Mixtures thereof. The silicate is preferably a neutral silicate.

The granulation is carried out according to the invention preferably at a product temperature of 40-60 ° C. The granulation can be carried out using commercial granulators, for example using fluidized bed granulators, in particular using spouted bed, Siebboden- or

Fluidized-bed granulators. Granulators which can be used according to the invention

for example, sold by the company Glatt (Binzen, Germany). By way of example, the granulator ProCell-LabSystem (Glatt, Germany) may be mentioned.

The agglomeration of the spray-dried particles is preferably carried out in one

Fluidized bed process using the aforementioned granulators. For this purpose, the fine, preferably spray-dried, powder is passed into the fluidized bed and there the agglomeration aid - preferably in dissolved form, for example as an aqueous solution - sprayed and thus finely distributed in the fluidized bed. The solvent is preferably evaporated by heating the incoming air. The supply air velocity is in this case preferably adjusted so that a turbulence of the agglomerated particles is possible. This is achieved by regulating the supply air volume. If the agglomerates reach the desired particle size, they are no longer fluidized due to their weight and can be taken out of the bottom of the fluidized bed or at the lateral outlet of the continuous fluidized bed. The residence time of the particles in the

Fluidized bed thus adjusts itself to the rate of particle growth, since the particles grow from the fine, spray-dried particle to the larger agglomerate need to leave the fluidized bed. The conditions to be used correspond to the standard conditions of thermal granulation.

In a biomass granulate according to the invention, the agglomeration aid is preferably present in an amount of from 0.05 to 6% by weight, in particular from 0.1 to 5.0% by weight, preferably from 0.2 to 4.5% by weight, in particular from 0.3 to 4.0% by weight, particularly preferably from 0.4 to 3.5% by weight, in particular from 0.5 to 3.2% by weight, in particular from 0.8 to 3.0% by weight .-%, in particular 1, 0 to 2.5 wt .-%, contained.

A particularly preferred biomass granules according to the invention contains carboxymethyl cellulose in an amount of 0.05 to 6 wt .-%, in particular 0.1 to 5 wt .-%, preferably 0.2 to 4.5 wt .-%, in particular 0.3 to 4.0 wt .-%, particularly preferably 0.4 to 3.5 wt .-%, in particular 0.5 to 3.2 wt .-%, especially 0.8 to 3.0 wt. -%, In particular 1, 0 to 2.5 wt .-%.

Contains another biomass granules particularly preferred according to the invention

Maltodextrins in an amount of 0.05 to 6 wt .-%, in particular 0.1 to 5 wt .-%, preferably 0.2 to 4.5 wt .-%, in particular 0.3 to 4.0 wt. %, particularly preferably 0.4 to 3.5 wt .-%, in particular 0.5 to 3.2 wt .-%, especially 0.8 to 3.0 wt .-%, in particular 1, 0 to 2, 5% by weight.

The agglomeration aid is metered into the process according to the invention in each case in an amount such that the stated wt .-% - proportion of

Agglomeration aids in the granules formed adjusts.

The biomass granules obtained when carrying out the granulation is preferably characterized in that the mean particle diameter (d50) is from 150 to 1000 μm.

The biomass granules obtained when carrying out the granulation are furthermore preferably characterized in that at least 80% by weight, in particular at least 90% by weight, particularly preferably at least 95% by weight, especially at least 98% by weight, the particles have a particle diameter (particle size) of 100 to 2000 μηη, preferably 100 to 1500 μηι, particularly preferably 100 to 1000 μηι have.

The particulate biomass used in the granulation process according to the invention can be obtained, for example, starting from biomass-containing fermentation broth by freeze drying or drum drying. However, it has turned out to be particularly advantageous according to the invention if particulate biomass obtained by spray-drying is used in the granulation process according to the invention. In spray drying, this is preferably

Used fermentation broth, optionally after prior concentration, the

contains corresponding biomass containing an oxidation-sensitive recyclable material. The spray drying can be carried out in a manner known to those skilled in the art, for example using a spray tower. In particular, a nozzle spray drying, in particular using a single-component nozzle or two-component nozzle, or drying using a rotating disk can be carried out. An example is the spray dryer Production Minor Spray Dryer (GEA Niro, Müllheim, Germany).

In a preferred embodiment, a hydrophilic or hydrophobic silicate is used in the spray drying of the biomass to obtain the particulate starting biomass. Alternatively or additionally, the hydrophilic or hydrophobic silicate can also be mixed in after the spray drying or else after the agglomeration. If used, the silicate is preferably used in an amount such that in the final granulation product a concentration of 0.05 to 5 wt.%, In particular 0.1 to 4 wt.%, Preferably 0.15 to 3.5 wt .-%, in particular 0.2 to 3.0 wt .-%, particularly preferably 0.25 to 2.5 wt .-%, in particular 0.3 to 2.0 wt .-%, especially 0.35 to 1, 8 wt .-%, in particular 0.4 to 1, 5 wt .-% adjusts. A biomass granules according to the invention is therefore distinguished, in another preferred embodiment according to the invention, by the fact that, besides the

Agglomeration aids further silicate, in particular hydrophobic and / or hydrophilic silicate, preferably in the amount indicated above, contains.

The preparation of the particulate starting biomass according to the invention is preferably carried out starting from a fermentation broth containing the biomass.

Before the spray-drying of the fermentation broth containing the biomass, it is also possible first to concentrate the fermentation broth containing the biomass in order to increase the solids content before the spray-drying. However, a prior restriction is not mandatory. If hydrophilic or hydrophobic silicate is used in the spray drying, the silicate is preferably only during the drying step or in the course of Drying method mixed with the fermentation broth or the still moist biomass. In the latter case, the silicate is preferably metered into the drying zone using a nozzle, preferably a two-substance nozzle. In the

Nozzle spray drying, the drying zone is the zone below the injection nozzle, through which the fermentation broth is metered. The silicate can in this case be metered in suspended form, but is preferably metered in dry, in particular pulverulent, form.

Hydrophilic silicas are under the CAS no. 1 12926-00-8 registered and commercially available, for example, under the trade name Sipernat® (Evonik Industries, Germany).

Hydrophilic silicas preferably used according to the invention have a specific surface area (ISO 9277) of from 130 to 600 m ² / g, preferably from 160 to 550 m ² / g, and preferably a dioctyl adipate absorption value of from 1.5 to 4.0 ml / g, preferably 2.0-3.2 ml / g. They also preferably have a tamped density (not sieved, based on ISO 787-1 1) of 80 to 300 g / l, preferably 100 to 270 g / l. The particle size of the hydrophilic silica (d50, laser diffraction, based on ISO 13320-1) is preferably 10 to 150 μm, in particular 15 to 130 μm. The drying loss of the hydrophilic silica (2 hours at 105 ° C., based on ISO 787-2) is preferably not more than 10%, particularly preferably not more than 7%. The loss on ignition of the hydrophobic silica (2 hours at 1000 ° C., based on ISO 3262-1) is preferably at most 10%, particularly preferably at most 6%. The silicon dioxide content of the hydrophilic silica is preferably at least 95% by weight, more preferably at least 97% by weight (based on ISO 3262-19). The pH of the hydrophilic silica (5% in water, based on ISO 787-9) is preferably from 5.0 to 7.0, more preferably from 6.0 to 6.5.

In a particularly preferred embodiment according to the invention, the hydrophilic silica is a product having a specific surface area of from 160 to 220 m ² / g, a dioctyl adipate absorption value of from 2.0 to 2.8 ml / g, a tapped density of from 200 to 300 g / l and a particle size of 100 to 150 μηη. Such a product is commercially available under the name Sipernat® 22 S (Evonik Industries, Germany).

In a further particularly preferred embodiment according to the invention, the hydrophilic silica is a product having a specific surface area of from 450 to 550 m ² / g, a dioctyl adipate absorption value of from 2.5 to 3.5 ml / g, a tapped density from 80 to 130 g / l and a particle size of 10 to 40 μηι. Such a product is commercially available under the name Sipernat® 50 S (Evonik Industries, Germany).

Hydrophobic silicas are under the CAS no. 6861 1 -44-9 registered and commercially, for example, also under the trade name Sipernat® (Evonik Industries,

Germany) available. Hydrophobic silicas preferably used according to the invention have a methanol wettability of at least 40%, preferably at least 45%, particularly preferably at least 50%, in particular 40 to 65%, especially 50 to 60%.

They also preferably have a tamped density (not sieved, based on ISO 787-1 1) of 100 to 200 g / l, preferably 125 to 175 g / l. The particle size of the

hydrophobic silica (d50; laser diffraction, based on ISO 13320-1) is preferably 5 to 15 μm, in particular 8 to 12 μm. The drying loss of

hydrophobic silica (2 hours at 105 ° C., based on ISO 787-2) is preferably not more than 10%, more preferably not more than 6%. The loss on ignition of the hydrophobic silica (2 hours at 1000 ° C., based on ISO 3262-1) is preferably at most 10%, particularly preferably at most 6%. The silicon dioxide content of the hydrophobic silica is preferably at least 95% by weight, more preferably at least 97% by weight (based on ISO 3262-19). The carbon content of the hydrophobic silica is preferably at most 3.5 wt .-%, in particular at most 2 wt .-% (based on ISO 3262-19). The pH of the hydrophobic silica (5% in a 1: 1 mixture of water and methanol, based on ISO 787-9) is preferably from 7 to 10.5, more preferably from 7.5 to 9.

The methanol wettability is a measure of the hydrophobicity of the silica powder. To determine this value, a certain amount of silica powder is weighed into water. The silica powder remains on the surface. The amount of methanol necessary for wetting the powder is then determined. Under

"Methanol wettability" is understood to mean the methanol content of a methanol-water mixture in% by volume, in which 50% of the hydrophobic silica sediment.

Hydrophobic silicas which can be used according to the invention are obtainable, for example, under the trade names Sipernat® D 10, Sipernat® D 15 and Sipernat® D 17 (Evonik Industries, Germany).

The fermentation broth used in the spray drying has before the start of

Spray drying preferably has a solids content of 10 to 50 wt .-% and according to a water content of 50 to 90 wt .-%,. If necessary, the fermentation broth is adjusted to this water content before the actual drying. This can be done in particular by centrifugation, flotation, 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 one-stage or multi-stage process. Alternatively, for example, the reverse osmosis for the purpose of narrowing the fermentation broth into consideration.

In this first optional but preferred step, the fermentation broth is preferably concentrated to a solids content of at least 10 or 15% by weight, preferably of at least 20 or 25% by weight, in particular 10 to 50 or 15 to 45% by weight. -%, particularly preferably 15 to 40 wt .-% or 20 to 40 wt .-%.

That the biomass to be dried to the particulate starting biomass is preferably present before the spray drying in the form of a suspension with the previously stated solids content, wherein the suspension is preferably fermentation broth or concentrated fermentation broth.

After the optional concentration of the fermentation broth, the drying of the biomass is now preferably carried out by spray drying, in particular by spray drying or spray drying using a rotating disk. Optionally, the biomass may also be subjected to the drying step immediately after harvesting without prior concentration, in particular if the obtained

Fermentation broth already has a high solids content, preferably as stated above.

The primary drying, preferably spray drying, of the biomass, this is preferably to a residual moisture content of at most 10 wt .-%, in particular 0 to 10 wt .-%, more preferably at most 8 wt .-%, in particular 0.5 to 8 wt. -%, especially at most 6 or 5 wt .-%, in particular 0.5 to 6 or 0.5 to 5 wt .-%, dried.

In the nozzle spray drying, the fermentation broth introduced is atomized into a defined drop size and dried with the introduced drying air in cocurrent. Since the individual droplets are separated from each other in this process, there is good heat and mass transport and thus efficient drying. In addition, over the set droplet size in the nozzle the particle size of the dried final product can be set defined.

If hydrophilic or hydrophobic silicate is used in the spray-drying, it is preferably atomized in the drying zone in order to avoid adhering the drying particles to each other. The silicate thus acts as a so-called anti-caking agent, whereby the setting of a defined and controllable particle size is facilitated.

In order to avoid the oxidation of the oxidation-sensitive valuable material as much as possible, the drying gas can be passed over the biomass during spray-drying if desired in a cycle gas mode. "Circular gas operation" means that the gas used for drying is circulated over the biomass in this case preferably has a temperature above the

Saturation temperature of the solvent to be evaporated. The gas used is preferably air, more preferably air having a reduced oxygen content. 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

To produce gas stream with reduced oxygen content.

The drying temperature in the nozzle spray tower can be adjusted to 95 ° C. because of the short residence times. "Solids content" is understood to mean the mass remaining after complete removal of the water , which only crystallize out or precipitate on drying, the solids content being so far complementary to the water or moisture content. The biomass-containing composition used in the drying is preferably the product of a fermentative cultivation process and is

accordingly also referred to as fermentation broth. The invention

to be used fermentation broth comprises in addition to the biomass to be dried

preferably further constituents of the fermentation medium. These ingredients may be, in particular, salts, antifoams and unreacted

Carbon source and / or nitrogen source act. During drying arises

preferably a product having a cell content of at least 60 wt .-%, preferably at least 65 wt .-%, in particular at least 70 or 80 wt .-%, wherein as further constituents, the silica and optionally the aforementioned further constituents of the fermentation medium and optionally partially released from the cells components are contained. If appropriate, the further constituents of the fermentation broth may be partially separated before the biomass is dried, for example by solid-liquid separation, so that a product is produced during the drying which contains these further components of the fermentation broth, in particular salts, preferably in a quantity of not more than 20 Wt .-%, in particular not more than 15, 10 or 5 wt .-%, contains.

The cells contained in the biomass are preferably cells which contain a valuable substance, preferably an oxidation-sensitive valuable substance. These may in particular be cells which naturally produce valuable substances, preferably lipids, in particular PUFAs (polyunsaturated fatty acids), but they may also be cells which are produced by appropriate genetic engineering

Methods have been enabled to produce lipids, in particular PUFAs. The production can be autotrophic, mixotrophic or heterotrophic. The biomass preferably comprises cells which produce lipids, in particular PUFAs, heterotrophically. According to the invention, the cells are preferably algae, fungi, in particular yeasts, or protists. Particularly preferred are cells of microbial algae or fungi.

Yeasts of Yarrowia, Candida, Rhodotorula, Rhodosporidium, Cryptococcus, Trichosporon and Lipomyces are particularly suitable as cells of oil-producing yeasts.

According to the invention, the biomass preferably comprises cells of the taxon

Labyrinthulomycetes (labyrinthulea, slime fungus, mucus), in particular those the family of Thraustochytriaceae. The family of Thraustochytriaceae includes the genera Althomia, Aplanochytrium, Elnia, Japonochytrium, Schizochytrium,

Thraustochytrium, Aurantiochytrium, Oblongichytrium and Ulkenia. The biomass particularly preferably comprises cells of the genera Thraustochytrium, Schizochytrium,

Aurantiochytrium or oblongichytrium, especially those of the genus Aurantiochytrium.

Within the genus Aurantiochytrium, the species Aurantiochytrium limacinum (formerly also called Schizochytrium limacinum) is preferred according to the invention. Very particular preference is given to using the strain Aurantiochytrium limacinum SR21 ((IFO 32693) according to the invention. 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).

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.

In a preferred embodiment, a large proportion of the 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.

Furthermore, 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.

According to the invention, polyunsaturated fatty acids (PUFAs) are fatty acids which have at least two, in particular at least three, CC double bonds. Among the PUFAs, according to the invention, highly unsaturated fatty acids (HUFAs) are preferred. According to the invention, HUFAs are fatty acids which have at least four CC 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,

in particular monoacyl, diacyl and triacylglycerides. In a preferred

Embodiment, 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 are eicosapentaenoic acid (EPA, 20: 5ω-3), in particular the (5Z, 8Z, 1 1 Z, 14Z, 17Z) eicosaccharide.

5,8,1,1,14,7-pentaenoic acid, and docosahexaenoic acid (DHA, 22: 6ω-3), in particular the (4Z, 7Z, 10Z, 13Z, 16Z, 19Z) docosa-4,7, 10, 13,16, 19-hexenoic acid, wherein the

Docosahexaenoic acid is particularly preferred.

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 (see, for example, WO91 / 07498, WO94 / 08467, WO97 / 37032, W097 / 36996, WO01 / 54510). The preparation is usually carried out by culturing cells in the presence of a carbon source and a nitrogen source in a fermenter. It can 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. 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 means, for example by limiting the nitrogen source, the carbon source or the oxygen content or combinations thereof.

The fermentation of the cells is preferably carried out in a medium with low salinity, in particular to prevent corrosion. This can be achieved in that, instead of sodium chloride, chlorine-free sodium salts, such as, for example, sodium sulfate,

Sodium carbonate, sodium bicarbonate or soda ash, can be used as sodium source. 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. Carbon sources are both alcoholic and non-alcoholic carbon sources. Examples of alcoholic carbon sources are methanol, ethanol and isopropanol. Examples of non-alcoholic carbon sources are fructose, glucose, sucrose, molasses, starch and corn syrup. Suitable sources of nitrogen include both inorganic and organic nitrogen sources. Examples of inorganic nitrogen sources are nitrates and ammonium salts, especially ammonium sulfate and ammonium hydroxide. Examples of organic

Nitrogen sources are amino acids, especially glutamate, and urea.

In addition, 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 3 to 1 1, in particular 4 to 10, and preferably at a temperature of at least 20 ° C, in particular 20 to 40 ° C, particularly preferably at least 30 ° C. A typical one

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

preferably by heating the biomass to a temperature of 50 to 121 ° C for a period of 5 to 60 minutes.

Likewise, after the biomass has been harvested or, if appropriate, also shortly before the harvest of the biomass, the addition of antioxidants is preferably carried out in order to protect the valuable material contained in the biomass from oxidative degradation. Preferred 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.

Particularly preferred according to the invention is a process for producing a particulate biomass, characterized in that a particulate starting biomass in

Presence of an agglomeration aid is granulated, so that the

Agglomeration aids in the final product in a concentration of 0.1 to 6 wt .-%, Preferably, 0.2 to 5 wt .-%, more preferably 0.5 to 4 wt .-%, especially 0.8 to 3 wt .-%, is contained, and wherein the biomass cells of the taxon Labyrinthulomycetes, in particular those of Family of Thraustochytriaceae, especially those of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, contains. Very particular preference is given to a process for producing a particulate biomass, characterized in that a particulate starting biomass in

Presence of an optionally modified polysaccharide as

Granulation agent is granulated so that the optionally modified

Polysaccharide in the final product in a concentration of 0.1 to 6 wt .-%, preferably 0.2 to 5 wt .-%, particularly preferably 0.5 to 4 wt .-%, especially 0.8 to 3 wt. -%, and wherein the biomass cells of the taxon Labyrinthulomycetes,

In particular, those of the family of Thraustochytriaceae, especially those of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium contains.

Very particular preference is given here to a process for producing a particulate biomass, characterized in that a particulate starting biomass is granulated in the presence of carboxymethyl cellulose as an agglomeration aid, so that the carboxymethyl cellulose in the final product in a concentration of 0, 1 to 6 wt .-%, preferably 0.2 to 5 wt .-%, particularly preferably 0.5 to 4 wt .-%, especially 0.8 to 3 wt .-%, is contained, and wherein the biomass Cells of the taxon

Labyrinthulomycetes, especially those of the family Thraustochytriaceae, especially those of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or

Oblongichytrium, in particular of the species Aurantiochytrium limacinum, especially of the strain Aurantiochytrium limacinum SR21.

Also particularly preferred is a method for producing a particulate biomass, characterized in that a particulate starting biomass is granulated in the presence of a maltodextrin, in particular a maltodextrin having a DE value of 3 to 10, as an agglomeration aid, so that the Maltodextrin in the final product in a concentration of 0.1 to 6 wt .-%, preferably 0.2 to 5

Wt .-%, particularly preferably 0.5 to 4 wt .-%, especially 0.8 to 3 wt .-%, is contained, and wherein the biomass cells of the taxon Labyrinthulomycetes, especially those of the family of Thraustochytriaceae, especially those of genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, in particular arose Aurantiochytrium limacinum, especially of the strain Aurantiochytrium limacinum SR21.

The particles produced by granulation according to the invention have excellent strength and have due to their low tendency to caking very good bulk and flow properties. The particles also have a low

Residual moisture and are preferably low in dust.

Granulation thus results in a free-flowing particulate product.

Optionally, a product having the desired grain size can be obtained from the granules obtained by sieving or dust separation. "Free-flowing" according to the invention is to be understood as meaning a powder which can flow out of a series of glass outlet vessels with differently sized outlet openings at least from the vessel with the opening 5 mm (Klein: Soaps, Oils, Fats, Wachse 94, 12 (1968)) ,

By "finely divided" is meant according to the invention a powder with a predominant proportion (> 50%) of a particle size of 20 to 100 micrometers in diameter.

Under "coarse-grained" according to the invention is a powder with a predominant proportion (> 50%) to understand a grain size of 100 to 2500 microns in diameter.

"Dust-free" according to the invention is to be understood as meaning a powder which only has small proportions (<10% by weight, preferably <5% by weight, in particular <3% by weight, especially <1% by weight) of particle sizes below 100 microns.

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 R. H. Müller and R. Schuhmann, Wissenschaftliche Verlagsgesellschaft 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 R.H. Müller and R. Schuhmann zur

Particle size measurement applied.

The products obtained by granulation processes according to the invention preferably have a proportion of at least 80 wt .-%, in particular at least 90 Wt .-%, particularly preferably at least 95 wt .-%, especially at least 98 wt .-%, of particles having a particle size of 100 to 2000 micrometers, preferably 100 to 1500 micrometers, in particular 100 to 1000 micrometers.

By contrast, the particulate starting biomass which is preferably obtainable by spray-drying processes preferably has a fraction of at least 80% by weight, in particular at least 90% by weight, particularly preferably at least 95% by weight, of particles having a particle size of from 100 to 500 micrometers. preferably 100 to 400 micrometers, especially 100 to 300 micrometers.

Due to the manufacturing process, a structure is formed, which is recognizable as an agglomerate of smaller particles. Preferably, at least 50 or 60 wt .-%, in particular at least 70 or 80 wt .-%, particularly preferably at least 90 or 95 wt .-%, in particular substantially all particles such an agglomerate structure.

At the same time, the particles according to the invention have a very low tendency to cake. This is presumably due to the agglomeration-related reduction in the surface-to-volume ratio of the particles. In this respect, in a preferred embodiment, the explicit addition of anti-caking agents - such as the aforementioned silicate - for the purpose of obtaining a free-flowing product can be completely dispensed with.

The proportion of dust, i. Particles having a particle size of less than 100 micrometers, is preferably at most 10 wt .-%, in particular at most 8 or 6 wt .-% particularly preferably at most 4 wt .-%, in particular at most 2 wt .-%.

The bulk density of the products according to the invention is preferably from 350 to 550 kg / m ³ , particularly preferably from 350 to 500 kg / m ³ , in particular from 350 to 450, kg / m ³ .

The agglomerate-structured particles preferably have a nonspherical geometry. In a preferred embodiment, therefore, at least 50 or 60% by weight, in particular at least 70 or 80% by weight, particularly preferably at least 90 or 95% by weight, in particular essentially all particles, are in non-spherical form.

In this case, "non-spherical" is to be understood as meaning that the diameter of a particle, starting from the center of mass of the particle, is not the same in all spatial directions, the deviation of the diameter of a particle starting from the center of mass of the particle being at least in relation to two spatial directions at least 20%, preferably at least 25%, more preferably at least 30%.

A particularly preferred object of the present invention is a particulate

Biomass containing an agglomeration aid in an amount of 0.05 to 6 wt .-%, in particular 0.1 to 5 wt .-%, preferably 0.2 to 4.5 wt .-%, in particular 0.4 to 4, 0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt .-%, especially 1, 0 to 3.0 wt .-%, in particular 1, 5 to 2.5 wt .-% and includes cells of the taxon Labynnthulomycetes, in particular those of the family of Thraustochytnaceae, especially those of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, in particular the species Aurantiochytrium limacinum, especially of the strain Aurantiochytrium limacinum SR21, contains, wherein at least 80 wt .-%, in particular at least 90 wt .-%, preferably at least 95 wt .-%, of the particles contained a particle size of 100 to 2000 micrometers, preferably 100 to 1500

Microns, especially 100 to 1000 microns have. Preference is given here in particular to a particulate biomass which contains an optionally modified polysaccharide in an amount of 0.05 to 6% by weight, in particular 0.1 to 5% by weight, preferably 0.2 to 4.5% by weight. , in particular 0.4 to 4.0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt .-%, especially 1, 0 to 3.0 Wt .-%, in particular 1, 5 to 2.5 wt .-% and cells of the taxon

Labynnthulomycetes, especially those of the family Thraustochytnaceae, especially those of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or

Oblongichytrium, in particular of the species Aurantiochytrium limacinum, especially of the strain Aurantiochytrium limacinum SR21, contains, wherein at least 80 wt .-%, in particular at least 90 wt .-%, preferably at least 95 wt .-%, of the particles contained a particle size of 100 to 2000 microns, preferably 100 to 1500

Microns, especially 100 to 1000 microns have.

In this case, particular preference is furthermore given to a particulate biomass which comprises a modified cellulose, in particular carboxymethyl cellulose, in an amount of from 0.05 to 6% by weight, in particular from 0.1 to 5% by weight, preferably from 0.2 to 4 , 5 wt .-%, in particular 0.4 to 4.0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt .-%, especially 1 , 0 to 3.0 wt .-%, in particular 1, 5 to 2.5 wt .-% and cells of the taxon Labynnthulomycetes, especially those of the family of Thraustochytnaceae, especially those of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, in particular of the species Aurantiochytrium limacinum, especially of the strain Aurantiochytrium limacinum SR21, contains, wherein at least 80 wt .-%, in particular at least 90 wt .-%, preferably at least 95 wt .-%, of the particles contained a particle size of 100 to 2000 microns, preferably 100 to 1500

Microns, especially 100 to 1000 microns have.

Particularly preferred is also a particulate biomass comprising a maltodextrin, in particular a maltodextrin having a DE value of from 3 to 10, in an amount of from 0.05 to 6% by weight, in particular from 0.1 to 5% by weight, preferably 0.2 to 4.5 wt .-%, in particular 0.4 to 4.0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt. %, especially 1, 0 to 3.0 wt .-%, in particular 1, 5 to 2.5 wt .-% and cells of the taxon Labyrinthulomycetes, in particular those of the family of

Thraustochytriaceae, especially those of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, in particular of the species Aurantiochytrium limacinum, in particular the strain Aurantiochytrium limacinum SR21, containing at least 80 wt .-%, in particular at least 90 wt .-%, preferably at least 95 Wt .-%, of the particles contained a particle size of 100 to 2000 micrometers, preferably 100 to 1500 micrometers, especially 100 to 1000 micrometers.

A particular subject of the present invention is a particulate biomass containing an optionally modified polysaccharide in an amount of 0.05 to 6 wt .-%, in particular 0.1 to 5 wt .-%, preferably 0.2 to 4.5 wt .-%, in particular 0.4 to 4.0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt .-%, especially 1, 0 bis 3.0 wt .-%, in particular 1, 5 to 2.5 wt .-% and cells of the taxon Labyrinthulomycetes, especially those of the family of Thraustochytriaceae, especially those of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, especially the species Aurantiochytrium limacinum, especially of the strain Aurantiochytrium limacinum SR21, wherein at least 80 wt .-%, in particular at least 90 wt .-%, preferably at least 95 wt .-%, of the particles contained a particle size of 100 to 2000 micrometers, preferably 100 until 1500

Microns, especially 100 to 1000 microns, wherein the biomass further comprises a hydrophilic or hydrophobic silicate in an amount of 0.05 to 6 wt .-%,

in particular from 0.1 to 5% by weight, preferably from 0.2 to 4.5% by weight, in particular from 0.4 to 4.0% by weight, particularly preferably from 0.6 to 3.5% by weight , in particular 0.8 to 3.2 wt .-%, especially 1, 0 to 3.0 wt .-%, in particular 1, 5 to 2.5 wt .-%, contains. In this case, in particular, a particulate biomass which is a modified biomass is preferred

Cellulose, in particular carboxymethyl cellulose, in an amount of 0.05 to 6 wt .-%, in particular 0.1 to 5 wt .-%, preferably 0.2 to 4.5 wt .-%, in particular 0.4 to 4.0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt .-%, especially 1, 0 to 3.0 wt .-%, in particular 1, 5 to 2.5 wt .-%, and includes cells of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, in particular the species Aurantiochytrium limacinum, especially the strain

Aurantiochytrium limacinum SR21, wherein at least 80 wt .-%, in particular at least 90 wt .-%, preferably at least 95 wt .-%, of the particles contained a particle size of 100 to 2000 microns, preferably 100 to 1500 microns, especially 100 to 1000 micrometers, and further comprising a hydrophilic or hydrophobic silicate in an amount of 0.05 to 6 wt .-%, in particular 0.1 to 5 wt .-%, preferably 0.2 to 4.5 wt. %, in particular 0.4 to 4.0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt .-%, especially 1, 0 to 3, 0 wt .-%, in particular 1, 5 to 2.5 wt .-%, contains.

Also particularly preferred is a particulate biomass comprising a maltodextrin, in particular a maltodextrin having a DE of from 3 to 10, in an amount of from 0.05 to 6% by weight, in particular from 0.1 to 5% by weight, preferably 0.2 to 4.5 wt .-%, in particular 0.4 to 4.0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt. -%, especially 1, 0 to 3.0 wt .-%, in particular 1, 5 to 2.5 wt .-%, and comprises cells of the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or

Microns, especially 100 to 1000 microns, and further comprising a hydrophilic or hydrophobic silicate in an amount of 0.05 to 6 wt .-%, in particular 0.1 to 5 wt .-%, preferably 0.2 to 4 , 5 wt .-%, in particular 0.4 to 4.0 wt .-%, particularly preferably 0.6 to 3.5 wt .-%, in particular 0.8 to 3.2 wt .-%, especially 1 , 0 to 3.0 wt .-%, in particular 1, 5 to 2.5 wt .-%, contains.

The particulate biomass 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, on site to produce a feed or food. A feed or food containing a particulate biomass according to the invention is therefore a further subject of the present invention.

Another object of the present invention is therefore also the use of a particulate biomass according to the invention for the production of a food or

Feed.

Another object of the present invention is therefore also a process for the preparation of a feed or food, in which an inventive particulate biomass is used and is preferably mixed with other food or feed ingredients. In order to increase the bioavailability of the PUFAs in the feed or foodstuff to be produced, the particulate biomass may, if appropriate, be subjected to a cell disruption method immediately before the production of the feed or food, as described in the applications WO2014 / 122087 or WO2014 / 122092.

Alternatively, however, the biomass can also be processed directly into a feed or foodstuff together with other feed or food components without prior cell disruption.

A particulate biomass according to the invention is preferably present in an amount of from 1 to 20% by weight, in particular from 3 to 15% by weight, in a feed or feed according to the invention. The particulate biomass according to the invention is used in a preferred embodiment according to the invention for the production of a food or feed in which the biomass is preferably mixed with other food or feed ingredients and then processed into the food or feed.

The processing of the mixture of biomass and other food or

Feed ingredients are in a preferred embodiment by a

Extrusion process to obtain ready-to-eat portions of the food or feed. Alternatively, for example, a pelleting process can also be used.

In the extrusion process, 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 Wave circulation speed of 100 - 1000 rpm, in particular 300 - 700 rpm performed. The residence time of the introduced mixture is preferably 5 to 30 seconds, in particular 10 to 20 seconds.

In a preferred embodiment of the extrusion process according to the invention, this comprises

Process 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 water vapor injection, in particular to effect the swelling of the starch preferably contained.

The other food or feed ingredients are preferably comminuted before mixing with the digested cells, if necessary

to ensure that a homogeneous mixture is obtained during the mixing step. The comminution of the other food or feed ingredients can be done, for example, using a hammer mill.

A preferred method for producing a food or feed according to the invention therefore comprises the following steps: a) provision of a particulate biomass which contains a valuable substance, preferably a lipid, more preferably omega-3 fatty acids, preferably by spray granulation of a fermentation broth; b) Granulation of the particulate biomass thus obtained with the addition of a

Agglomerationshilfsmittels, wherein as granulation preferably modified cellulose, in particular carboxymethylcellulose, or a maltodextrin, in particular a maltodextrin having a DE value of 3 to 10, is used, so that the

Agglomeration aids in the granulation product in an amount of 0.1 to 6 wt .-%, preferably 0.2 to 5 wt .-%, particularly preferably 0.5 to 4 wt .-%, is included; c) mixing of the particulate biomass from (b), optionally after previous implementation of a cell disruption method, with further food or

Feed ingredients; d) Preparation of the final product by a compaction or extrusion process. An inventively very particularly preferred method for producing a

Food or feed comprises the following steps: a) provision of a particulate biomass, the slime fungi, in particular those of the family Thraustochytriaceae, especially those of the genera Thraustochytrium,

Schizochytrium, Aurantiochytrium or Oblongichytrium, contains; b) Granulation of the particulate biomass thus obtained with the addition of a

Agglomeration aids in the granulation product in an amount of 0.1 to 6 wt .-%, preferably 0.2 to 5 wt .-%, is included; c) mixing of the particulate biomass from (b), optionally after previous

Carrying out a cell disruption method, with other food or

Feed ingredients; d) Preparation of the final product by a compaction or extrusion process.

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

Suspension. In this way, it is additionally ensured that the contained valuable material is harmed as little as possible.

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

Production of the food or feed composition used.

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 further fatty-containing components and furthermore from others

Additives such as minerals, vitamins, pigments and amino acids. Besides nutrient substances, structuring substances may also be present in order to improve the texture or the appearance of the feedstuff. Furthermore, for example, binders can be used to influence the consistency of the feed. A preferred component that is both a nutrient and a structurant is starch.

As a protein-containing component, which additionally contains fats, can be used, for example, fish meal, krill flour, shellfish, squid or Schrimpsschalen. Alternatively, fish oil can be used as a fat-containing component. As a fat-containing component can also be used a vegetable oil, in particular oil from soybeans, rapeseeds, sunflower seeds and flaxseed. As 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

To breed 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 preferred salmon species are Atlantic salmon, red salmon, masu salmon, king salmon, keta salmon, silver salmon, Danube salmon, pacific salmon and humpback salmon. Alternatively, it may be a feed intended for the cultivation of Fish, which are then processed into fishmeal or fish oil. The fish are preferably herring, pollack, menhaden, anchovies, capelin or cod. The 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

Stock up on wild fish stocks.

In salmon farming, it is preferable first to cultivate herbs to fresh salmon in freshwater tanks or artificial streams of water and then to continue breeding in the sea in floating cages or net pens, which are preferably anchored in bays or fjords.

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.

embodiments

Example 1 Production of Spray-Dried Biomass For the production of DHA, the strain Aurantiochytrium limacinum SR21 was used. This is deposited with NIBH under FERM BP-5034 and IFO under IFO 32693. Strain A. limacinum SR21 was originally isolated from seawater and named Schizochytrium limacinum SR21 (Nakahara et al., 1996, JAOCS, 73 (10); Honda Mycol. Res. 1998). Due to reclassification, he was assigned to the new genus Aurantiochytrium and renamed accordingly.

The fermentation of the strain was carried out in a medium containing 50% artificial

Sea water (Sigma Aldrich) and which further contained the following components: 60 g / l glucose, 0.7 g / l corn steep liquor (Sigma Aldrich), 2 g / l (NH ₄ ) ₂ S0 ₄ and 3 g / l KH ₂ P0 , The fermentation was carried out at 28 ° C, a pH of 4.0, a ventilation rate of 0.5 vvm and a stirring of 200 rpm for 60 hours. After completion of the fermentation, an antioxidant was added to the fermentation broth and the fermentation broth was then heated to 60 ° C for at least 20 minutes. This was followed by a two-stage drying of the biomass: First, the fermentation broth was concentrated by evaporation to a dry mass of about 20 wt .-%. Subsequently, spray drying of the concentrated fermentation broth was carried out using a Production Minor ™ Spray Dryer (GEA NIRO) at one

Inlet temperature of the drying air of 340 ° C. By spray-drying, a powder having a dry matter content of more than 95% by weight was thus obtained.

Example 2: Granulation of spray-dried biomass using

Carboxymethylcellulose as agglomeration aid

For the agglomeration of the spray-dried particles from Example 1, the granulator ProCell-LabSystem (Glatt, Germany) was used to carry out a fluidized-bed granulation. The GF3 insert was used here. The fine, spray-dried biomass powder was passed into the fluidized bed and sprayed there a carboxymethylcellulose solution (4 wt .-% Blanose, dissolved in water) and thus fine in the

Distributed fluidized bed, so that a final concentration of carboxymethylcellulose of 3 wt .-% set. The solvent was evaporated by heating the supply air to 60 ° C. The supply air velocity was adjusted so that a turbulence of the agglomerated particles is possible. This was achieved by regulating the supply air to about 80 m ³ / h. As soon as the agglomerates reached the desired particle size, they were no longer fluidized due to their weight and could be removed at the lower end of the fluidized bed. The residence time of the particles in the fluidized bed was thus adjusted by the rate of particle growth, since the particles had to grow from the fine, spray-dried particle to the larger agglomerate in order to increase the particle size

Leave fluidized bed.

The specified conditions corresponded to the standard conditions of a thermal granulation. The product thus obtained showed in comparison to the starting biomass significantly improved product properties, in particular a significantly improved flowability.

Example 3: Granulation of spray-dried biomass using maltodextrin DE 3.5 as agglomeration aid

For the agglomeration of the spray-dried particles from Example 1, the granulator ProCell-LabSystem (Glatt, Germany) was used to carry out a fluidized-bed granulation. The GF3 insert was used here. The fine, spray-dried biomass powder was passed into the fluidized bed where a maltodextrin DE 3.5 solution (25% by weight of maltodextrin DE 3.5, dissolved in water) was sprayed and thus finely distributed in the fluidized bed, so that a final concentration of maltodextrin DE 3.5 of 3% by weight. The solvent was evaporated by heating the supply air to 60 ° C. The supply air velocity was adjusted so that a turbulence of the agglomerated particles is possible. This was achieved by regulating the supply air to about 80 m ³ / h. As soon as the agglomerates reached the desired particle size, they were no longer fluidized due to their weight and could be removed at the lower end of the fluidized bed. The residence time of the particles in the fluidized bed was thus adjusted by the rate of particle growth, since the particles had to grow from the fine, spray-dried particle to the larger agglomerate in order to increase the particle size

Leave fluidized bed.

The specified conditions corresponded to the standard conditions of a thermal granulation.

The product thus obtained showed in comparison to the starting biomass significantly improved product properties, in particular a significantly improved flowability.

Example 4: Granulation of spray-dried biomass using maltodextrin 18.9 as agglomeration aid

For the agglomeration of the spray-dried particles from Example 1, the granulator ProCell-LabSystem (Glatt, Germany) was used to carry out a fluidized-bed granulation. The GF3 insert was used here. The fine, spray-dried Biomass powder was passed into the fluidized bed and there sprayed a maltodextrin 18.9 solution (40 wt .-% maltodextrin 18.9, dissolved in water) and thus fine in the

Fluidized bed distributed so that a final concentration of maltodextrin 18.9 of 3 wt .-% adjusted. The solvent was evaporated by heating the supply air to 60 ° C. The supply air velocity was adjusted so that a turbulence of the agglomerated particles is possible. This was achieved by regulating the supply air to about 80 m ³ / h. As soon as the agglomerates reached the desired particle size, they were no longer fluidized due to their weight and could be removed at the lower end of the fluidized bed. The residence time of the particles in the fluidized bed was thus adjusted by the rate of particle growth, since the particles had to grow from the fine, spray-dried particle to the larger agglomerate in order to increase the particle size

Leave fluidized bed.

Claims

claims

Process for producing a particulate biomass containing a

contains oxidation-sensitive recyclable material, characterized in that a particulate starting biomass is subjected to a granulation process in the presence of an agglomeration aid.

A method according to claim 1, characterized in that as

Agglomeration aids optionally modified carbohydrates, in particular optionally modified polysaccharides, are used.

A method according to claim 2, characterized in that as

Agglomeration aids guar gum, gum arabic, guar gum, locust bean gum, xanthan gum, agar, carrageenan, a maltodextrin, starch, in particular

Corn starch, tapioca starch or potato starch, cellulose or its derivatives, hemicellulose or its derivatives, alginic acid or maltodextrin, or mixtures thereof.

A method according to claim 3, characterized in that as

Agglomerationshilfsmittel modified cellulose, especially carboxymethyl cellulose and / or hydroxypropylmethyl cellulose, or a maltodextrin or mixtures thereof can be used.

Method according to one of the preceding claims, characterized in that proteins are used as agglomeration aids, in particular casein, gelatin, collagen, wheat gluten or mixtures thereof.

Method according to one of the preceding claims, characterized in that organic polymers are used as agglomeration aids, in particular lignosulfonates, Polymethylolcarbamide, polyacrylic acids or

Polyvinyl alcohols or mixtures thereof.

Method according to one of the preceding claims, characterized in that inorganic substances are used as agglomeration aids, in particular silicates, preferably bentonites, hexametaphosphate or mixtures thereof.

Method according to one of the preceding claims, characterized in that the particulate starting biomass was obtained by spray-drying a fermentation broth containing the biomass.

Method according to one of the preceding claims, characterized in that the biomass cells of the taxon Labyrinthulomycetes, in particular those of the family of Thraustochytriaceae, particularly preferably of the genera

Thraustochytrium, Schizochytrium, Aurantiochytrium, Oblongichytrium or Ulkenia, especially the genus Aurantiochytrium, contains.

10. The method according to any one of the preceding claims, characterized in that it is the oxidation-sensitive recyclable PUFAs, preferably omega-3 fatty acids, more preferably DHA, is.

1 1. Particulate biomass containing an oxidation-sensitive valuable material, characterized in that it contains an agglomeration aid in an amount of 0.05 to 6 wt .-%, in particular 0.1 to 5 wt .-%, particularly preferably 0.4 to 4 wt. -%, contains.

12. Particulate biomass according to claim 11, characterized in that the agglomeration aid is an optionally modified carbohydrate, preferably a modified cellulose, more preferably

Carboxymethyl cellulose or hydroxypropylmethyl cellulose, or to a

Maltodextrin or mixtures thereof.

13. Particulate biomass according to claim 1 1 or 12, characterized in that it contains a hydrophilic or hydrophobic silicate in an amount of 0.05 to 6 wt .-%, preferably 0.1 to 5 wt .-%.

14. Particulate biomass according to any one of claims 1 1 to 13, characterized in that at least 80 wt .-%, in particular at least 90 wt .-%, preferably at least 95 wt .-%, of the particles has a particle diameter (particle size) of 100 to 2000 μηι, preferably 100 to 1500 μηι, more preferably 100 to 1000 μηη have.

15. Particulate biomass according to one of claims 1 to 14, characterized in that it cells of the taxon Labyrinthulomycetes, especially those of the family of Thraustochytriaceae, particularly preferably the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, especially the genus Aurantiochytrium, in particular the Species Aurantiochytrium limacinum. 16. Particulate biomass according to any one of claims 1 to 15, characterized in that it is the oxidation-sensitive recyclable PUFAs, preferably omega-3 fatty acids, more preferably DHA, is.

17. food or food containing a particulate biomass according to any one of claims 1 1 to 16.