Patent Grant
11464244
The present application is US national stage of international application PCT/EP2015/071666, which had an international filing date of Sep. 22, 2015, and which was published in German under PCT Article 21(2) on Apr. 7, 2016. Priority is claimed to European application EP 14187485.9, filed on Oct. 2, 2014.
The present invention relates to a PUFA (polyunsaturated fatty acid)-containing feedstuff having high abrasion resistance and high water stability.
Processes for producing PUFA-containing biomass have already been described in the prior art. PUFA-containing biomass together with other feedstuff ingredients can be further processed by, for example, extrusion.
It is desirable for the feedstuff obtained to have particular product properties. For instance, it is advantageous for each feedstuff to have a high abrasion resistance. This is because high abrasion resistance means in particular that damage to the feedstuff during transport can be largely prevented.
Especially for a feedstuff in aquaculture, it is additionally desirable for it to have a high water stability, i.e. for it to remain intact for as long as possible after addition to water and thus be available as feedstuff to the fish for a prolonged period.
It is therefore an object of the present invention to provide a PUFA-containing feedstuff having improved product properties, in particular having a high abrasion resistance and/or a high water stability.
According to the invention, it was found that, surprisingly, a feedstuff having a very high abrasion resistance and very high water stability can be obtained when, during the production of the feedstuff, use is made of a Labyrinthulea biomass obtained by culturing in a concentration of sulphate such that the resulting biomass, with regard to the dry mass, has a sulphate content of 25 to 60 g/kg, in particular 25 to 50, 25 to 40 or 25 to 35 g/kg.
If another biomass or fish oil is used as PUFA source instead of the Labyrinthulea biomass to be used according to the invention, a feedstuff having a distinctly lower abrasion resistance and a distinctly lower water stability is obtained.
The present invention therefore firstly provides a feedstuff containing PUFAs, characterized in that it has an abrasion resistance of at least 91%. The abrasion resistance is preferably at least 92 or 93%, especially preferably at least 94%.
The present invention therefore also further provides a feedstuff containing PUFAs, characterized in that it has a water stability of at least 96%. The water stability is preferably at least 97%, especially preferably at least 98%.
The feedstuff is produced by extrusion. Extrusion is preferably followed by coating of the extrudate with oil. The abrasion resistance of the feedstuff was determined using the uncoated extrudate; by contrast, the water stability of the feedstuff was carried out using the extrudate subsequently coated with oil.
The present invention therefore also further provides a process for producing a feedstuff, in particular extrudate, according to the invention, characterized in that a PUFA-containing biomass having a sulphate content of 25 to 60 g per kilogram of biomass and preferably obtained as indicated above is extruded together with other feedstuff components and, optionally, the extrudate thus obtained is loaded with oil, preferably after being dried beforehand.
Abrasion resistance is determined by exposing the sample to a mechanical agitation and then determining the amount of fine particles detached from the sample. According to the invention, abrasion resistance was determined as follows: The dried extrudate (having a diameter of 4 mm and a length of 4 mm) was exposed to a mechanical load using the Holmen pellet tester NH P100 (Borregaard Lignotech, Hull, UK). Before carrying out the test, the samples were screened in order to remove any adherent fine particles. The processed samples (100 g) were subsequently introduced into the pellet tester using a 2.5 mm filter screen. The pellets were subsequently conveyed through a pipe having right-angled pipe bends at high air velocity (about 70 mbar) for 30 seconds. The experimental parameters are predetermined by the equipment. Subsequently, abrasion was determined by weighing. Abrasion resistance was specified as PDI (Pellet Durability Index), defined as the amount in percent of sample remaining in the filter screen after the test has been carried out. The test was carried out with three samples and then the mean was determined.
Water stability was determined using the oil-loaded samples. The method was essentially carried out as described by Baeverfjord et al. (2006; Aquaculture 261, 1335-1345), with slight modifications. 10 g samples of the extrudate (having a length and a diameter of 4 mm in each case) were introduced into metallic infusion baskets (Inox, Germany) having a diameter of 6.5 mm and a mesh size of 0.3 mm. The infusion baskets were subsequently introduced into a plastic trough containing water, and so the samples were completely covered with water. The trough was subsequently exposed for 30 minutes to a shake-agitation of 30 shake units per minute using the Multiorbital shaker PSU-201 (Biosan, Latvia). Thereafter, the samples were carefully dried with blotting paper and then weighed before and after they had been subjected to oven-drying at a temperature of 105° C. for 24 hours. Water stability was calculated as the difference in the dry weight of the sample before and after the incubation in water and specified in percent of the dry weight of the sample used before the incubation with water.
The feedstuff according to the invention preferably has a bulk density of 400 to 600 g/l.
A feedstuff according to the invention is preferably obtained by extrusion of a feedstuff composition containing a Labyrinthulea biomass to be used according to the invention.
For setting the desired abrasion resistance and water stability, it proved to be especially advantageous according to the invention when the extrusion is done at an energy input of 12-28 Wh/kg, in particular 14-26 Wh/kg, especially preferably 16-24 Wh/kg, above all 18-22 Wh/kg.
In this connection, a screw or twin-screw extruder is preferably employed in the extrusion process. The extrusion process is preferably carried out at a temperature of 80-220° C., in particular 80-130° C., above all 95-110° C., a pressure of 10-40 bar, and a shaft rotational speed of 100-1000 rpm, in particular 300-700 rpm. The residence time of the mixture introduced is preferably 5-30 seconds, in particular 10-20 seconds.
The extrusion process may optionally comprise a compacting step and/or a compression step.
It is preferred to intimately mix the components with each other before carrying out the extrusion process. This is preferably carried out in a drum equipped with vanes. In a preferred embodiment, this mixing step includes an injection of steam, in particular so as to bring about swelling of the starch which is preferably present. In this case, the injection of steam is carried out preferably at a pressure of 1 to 5 bar, especially preferably at a pressure of 2 to 4 bar.
Before being mixed with the algae biomass, the further foodstuff or feedstuff ingredients are preferably comminuted—if required—so as to ensure that a homogeneous mixture is obtained in the mixing step. The comminuting of the further foodstuff or feedstuff ingredients may be carried out, for example, using a hammer mill.
The extrudate created preferably has a diameter of 1 to 14 mm, preferably 2 to 12 mm, in particular 2 to 6 mm, and preferably also has a length of 1 to 14 mm, preferably 2 to 12 mm, in particular 2 to 6 mm. The length of the extrudate is set during extrusion by using a cutting tool. The length of the extrudate is preferably selected such that it approximately corresponds to the diameter of the extrudate. The diameter of the extrudate is defined by selecting the screen diameter.
In one embodiment preferred according to the invention, the extrusion process is followed by the extrudate obtained being loaded with oil. To this end, the extrudate is preferably initially dried to a moisture content of at most 5% by weight. According to the invention, the extrusion product may be loaded with oil by, for example, placing the extrudate in oil or spraying the extrudate with oil; however, according to the invention, preference is given to vacuum coating.
Production of Labyrinthulea biomasses usable according to the invention has been described in detail in the prior art. The specific part of the invention is that a Labyrinthulea biomass having a very high sulphate content is used in order to produce feedstuff according to the invention. In this way, a biomass having a very high content of exopolysaccharides is obtained. It is presumed that this ultimately leads to the extruded feedstuff having such a high abrasion resistance and water stability.
The cells of the taxon Labyrinthulea that are usable according to the invention are also called Labyrinthulomycetes or slime nets. Labyrinthulea which are preferably used belong to the family of the Thraustochytriaceae. The family of the Thraustochytriaceae includes the genera Althomia, Aplanochytrium, Elnia, Japonochytrium, Schizochytrium, Thraustochytrium, Aurantiochytrium, Oblongichytrium and Ulkenia. The biomass particularly preferably comprises cells from the genera Thraustochytrium, Schizochytrium, Aurantiochytrium or Oblongichytrium, above all those from the genus Aurantiochytrium.
Within the genus Aurantiochytrium, preference is given, according to the invention, to the species Aurantiochytrium limacinum (previously also known as Schizochytrium limacinum). According to the invention, very particular preference is given to using the strain Aurantiochytrium limacinum SR21.
According to the invention, polyunsaturated fatty acids (PUFAs) are understood to mean fatty acids having at least two, particularly at least three, C—C double bonds. According to the invention, highly unsaturated fatty acids (HUFAs) are preferred among the PUFAs. According to the invention, HUFAs are understood to mean fatty acids having at least four C—C double bonds.
The PUFAs may be present in the cell in free form or in bound form. Examples of the presence in bound form are phospholipids and esters of the PUFAs, in particular monoacyl-, diacyl- and triacylglycerides. In a preferred embodiment, the majority of the PUFAs is present in the form of triglycerides, with preferably at least 50% by weight, in particular at least 75% by weight and, in an especially preferred embodiment, at least 90% by weight of the PUFAs present in the cell being present in the form of triglycerides.
Preferred PUFAs are omega-3 fatty acids and omega-6 fatty acids, with omega-3 fatty acids being especially preferred. Preferred omega-3 fatty acids in this context are eicosapentaenoic acid (EPA, 20:5ω-3), in particular (5Z,8Z,11Z,14Z,17Z)-eicosa-5,8,11,14,17-pentaenoic acid, and docosahexaenoic acid (DHA, 22:6ω-3), in particular (4Z,7Z,10Z,13Z,16Z,19Z)-docosa-4,7,10,13,16,19-hexaenoic acid, with docosahexaenoic acid being especially preferred.
The cells present in the biomass are preferably distinguished by the fact that they have a PUFA content, preferably DHA content, of at least 20% by weight, preferably at least 25% by weight, in particular at least 30% by weight, based in each case on the cell dry mass, with preferably at least 50% by weight, in particular at least 75% by weight and, in an especially preferred embodiment, at least 90% by weight of the lipids present in the cell being present in the form of triglycerides.
The other feedstuff ingredients are preferably selected from protein-containing, carbohydrate-containing, nucleic-acid-containing and lipid-soluble components and, if appropriate, further fat-containing components and furthermore from among other additives such as minerals, vitamins, pigments and amino acids. Besides, structurants may also be present, besides nutrients, for example so as to improve the texture or the appearance of the feedstuff. Furthermore, it is also possible to employ, for example, binders so as to influence the consistency of the feedstuff. A component which is preferably employed and which constitutes both a nutrient and a structurant is starch.
In a preferred embodiment, the extrudate obtained is subsequently coated with oil. In this respect, a distinction has to be made according to the invention between uncoated extrudate and extrudate subsequently coated with oil. The extrudate is, with regard to the final product, preferably coated with 3 to 18% by weight, in particular 5 to 15% by weight, above all 7 to 13% by weight, of oil. The extrudate is preferably coated with oil by vacuum evaporation.
According to the invention, a feedstuff according to the invention having an abrasion resistance of at least 91% is preferably distinguished by the fact that it contains a Labyrinthulea biomass in an amount of 2 to 24% by weight, preferably 4 to 22% by weight, in particular 9 to 20% by weight, above all 11 to 18% by weight.
Said feedstuff preferably additionally has at least one, preferably all, of the following properties:
The invention therefore preferably provides a feedstuff, in particular extrudate, having an abrasion resistance of at least 91, 92, 93 or 94% and additionally having at least one, preferably all, of the following properties:
The invention therefore also preferably provides a feedstuff, in particular extrudate, having an abrasion resistance of at least 91, 92, 93 or 94% and additionally having at least one, preferably all, of the following properties:
The invention therefore also preferably provides a feedstuff, in particular extrudate, having an abrasion resistance of at least 91, 92, 93 or 94% and additionally having at least one, preferably all, of the following properties:
Accordingly, compositions having the features mentioned in the lists shown above are preferably used for producing feedstuff according to the invention having high abrasion resistance.
According to the invention, a feedstuff according to the invention having an abrasion resistance of at least 91% is accordingly preferably obtained by extrusion of a feedstuff mixture containing the above-mentioned components, with the extrusion preferably being carried out as described above, in particular at an energy input of 12-28 Wh/kg, in particular 14-26 Wh/kg, especially preferably 16-24 Wh/kg, above all 18-22 Wh/kg.
According to the invention, a feedstuff according to the invention having a water stability of at least 96% is preferably likewise obtained by extrusion of a feedstuff mixture containing the above-mentioned components, with the extrusion likewise preferably being carried out as described above, in particular at an energy input of 12-28 Wh/kg, in particular 14-26 Wh/kg, especially preferably 16-24 Wh/kg, above all 18-22 Wh/kg, with the extrusion process being followed by coating of the extrudate with oil in an amount of 3 to 18% by weight, in particular 5 to 15% by weight, above all 7 to 13% by weight, with regard to the final product.
According to the invention, a feedstuff according to the invention having a water stability of at least 96% is preferably distinguished by the fact that it contains a Labyrinthulea biomass in an amount of 2 to 22% by weight, preferably 4 to 20% by weight, in particular 8 to 18% by weight, above all 10 to 16% by weight.
Said feedstuff preferably additionally has at least one, preferably all, of the following properties:
The invention therefore also preferably provides a feedstuff, in particular extrudate, having a water stability of at least 96, 97 or 98% and additionally having at least one, preferably all, of the following properties:
The invention therefore also preferably provides a feedstuff, in particular extrudate, having a water stability of at least 96, 97 or 98% and additionally having at least one, preferably all, of the following properties:
The invention therefore also preferably provides a feedstuff, in particular extrudate, having a water stability of at least 96, 97 or 98% and additionally having at least one, preferably all, of the following properties:
According to the invention, the fat-containing component used may be, besides the biomass to be used according to the invention, fats, in particular oils, of both animal and plant origin. According to the invention, suitable fat-containing components are in particular vegetable oils, for example soya bean oil, rapeseed oil, sunflower seed oil, flaxseed oil or palm oil and mixtures thereof. In addition, fish oil may also optionally be used as fat-containing component in low amounts.
Preferably, a feedstuff according to the invention having a water stability of at least 96, 97 or 98% contains vegetable oils in an amount of 3 to 18% by weight, in particular 5 to 15% by weight, above all 7 to 13% by weight. As described above, the vegetable oil is in this connection preferably applied to the extrudate in a subsequent manner, in particular by vacuum coating.
According to the invention, the protein-containing component used may be, for example, soya protein, pea protein, wheat gluten or corn gluten and mixtures thereof.
The following examples may be employed as a protein-containing component which additionally contains fats: fish meal, krill meal, bivalve meal, squid meal or shrimp shells. These are hereinafter subsumed under the term “marine meal”. In a preferred embodiment, a feedstuff according to the invention comprises marine meal, preferably fish meal, in an amount of 3 to 18% by weight, in particular 5 to 15% by weight, above all 7 to 13% by weight.
The carbohydrate-containing component used may be, for example, wheat meal, sunflower meal or soya meal and mixtures thereof.
The foodstuff or feedstuff is preferably a product for use in aquaculture or a foodstuff or feedstuff for use in poultry production, pig production or cattle production. The feedstuff may also take the form of a feedstuff which is employed for growing small organisms which may be employed as feedstuff in aquaculture. The small organisms may take the form of, for example, nematodes, crustaceans or rotifers. The feedstuff is preferably present in the form of flakes, spheres or tablets. A feedstuff obtainable by extrusion has a moisture content of preferably less than 5% by weight, especially preferably 0.2 to 4% by weight.
The feedstuff for use in aquaculture is preferably used for breeding finish and crustaceans which are preferably intended for human nutrition. These include, in particular, carp, tilapia, catfish, tuna, salmon, trout, barramundi, bream, perch, cod, shrimps, lobster, crabs, prawns and crayfish. It is especially preferably a feedstuff for salmon farming. Preferred types of salmon in this context are the Atlantic salmon, red salmon, masu salmon, king salmon, keta salmon, coho salmon, Danube salmon, Pacific salmon and pink salmon.
Alternatively, it may also be a feedstuff intended for farming fish which are subsequently processed to give fish meal or fish oil. In this connection, the fish are preferably herring, pollack, menhaden, anchovies, capelin or cod. The fish meal or fish oil thus obtained, in turn, can be used in aquaculture for farming edible fish or crustaceans.
Aquaculture may take place in ponds, tanks, basins or else in segregated areas in the sea or in lakes, in particular in this case in cages or net pens. Aquaculture may be used for farming the finished edible fish, but also may be used for farming fry which are subsequently released so as to restock the wild fish stocks.
In salmon farming, the fish are preferably first grown into smolts in freshwater tanks or artificial watercourses and then grown on in cages or net pens which float in the sea and which are preferably anchored in bays or fjords.
Accordingly, the present invention also further provides a method for farming animals, in particular finfish or crustaceans, preferably salmon, in which a feedstuff according to the invention is employed. The present invention additionally further provides an animal, in particular a finfish or shellfish, which is obtainable by such a method according to the invention.
Processes for production of biomass, particularly that biomass which contains cells comprising lipids, particularly PUFAs, particularly from the order Thraustochytriales, are described extensively in the prior art. As a rule, the production takes place by cells being cultured in a fermenter in the presence of a carbon source and of a nitrogen source. In this context, biomass densities of more than 100 grams per litre and production rates of more than 0.5 gram of lipid per litre per hour may be attained. The process is preferably carried out as what is known as a fed-batch process, i.e. the carbon and nitrogen sources are fed in incrementally during the fermentation. Once the desired biomass has been obtained, lipid production may be induced by various measures, for example by limiting the nitrogen source, the carbon source or the oxygen content or combinations of these.
Preferably, the cells are fermented in a medium with low salinity, in particular so as to avoid corrosion. This can be achieved by employing chlorine-free sodium salts as the sodium source instead of sodium chloride, such as, for example, sodium sulphate, sodium carbonate, sodium hydrogen carbonate or soda ash. Preferably, chloride is employed in the fermentation in amounts of less than 3 g/l, in particular less than 500 mg/l, especially preferably less than 100 mg/l.
Suitable 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 nitrogen sources are both inorganic and organic nitrogen sources. Examples of inorganic nitrogen sources are nitrates and ammonium salts, in particular ammonium sulphate and ammonium hydroxide. Examples of organic nitrogen sources are amino acids, in particular glutamate, and urea.
In addition, inorganic or organic phosphorus compounds and/or known growth-stimulating substances such as, for example, yeast extract or corn steep liquor, may also be added so as to have a positive effect on the fermentation.
The amount of sulphate added during fermentation is selected such that a sulphate content of 25 to 60 g/kg, in particular 25 to 50, 25 to 40 or 25 to 35 g/kg, with regard to the dry mass, ensues in the resulting biomass.
According to the invention, the sulphate content in the resulting biomass may be set in different ways.
For example, in what is known as a batch process, the required amount of sulphate may be initially charged in full right at the start. The amount of sulphate required can be easily calculated, since the cells used to form the biomass virtually completely assimilate the sulphate.
When using what is known as a fed-batch process, the amount of sulphate required may alternatively be metered in during the course of fermentation or, accordingly, some of the sulphate may be initially charged and the remainder metered in during the course of fermentation.
Especially when it emerges during the course of fermentation that the amount of biomass produced exceeds the originally calculated value, it is possible to ensure by subsequent metering-in of sulphate that the resulting biomass contains the required amount of sulphate.
The sulphate salt used is preferably sodium sulphate. The chloride content during fermentation is preferably less than 3 g/l, in particular less than 500 mg/l, especially preferably less than 100 mg/l. In addition to sulphates and any chlorides used, it is also optionally possible during fermentation to use further salts, especially those selected from sodium carbonate, sodium hydrogen carbonate, soda ash or inorganic phosphorus compounds. If further salts are used, these are preferably likewise each used in an amount of less than 3 g/l, in particular less than 500 mg/l, especially preferably less than 100 mg/l. The total salt content in the fermentation medium is preferably 15 to 25 g/l, in particular 17 to 21 g/l.
The sulphate salt used is preferably sodium sulphate, ammonium sulphate or magnesium sulphate and also mixtures thereof.
During fermentation, the chloride content is, with regard to the liquid fermentation medium including the biomass present, preferably always below 3 g/kg, in particular below 1 g/kg, especially preferably below 400 mg/kg of fermentation medium.
In addition to sulphates and any chlorides used, it is also optionally possible during fermentation to use further salts, especially those selected from sodium carbonate, sodium hydrogen carbonate, soda ash or inorganic phosphorus compounds.
If further salts are used, these are preferably used in an amount such that each one during fermentation, with regard to the liquid fermentation medium including the biomass present, is present in each case in an amount of less than 10 g/kg, in particular less than 5 g/kg, especially preferably less than 3 g/kg in the fermentation medium.
According to the invention, the total salt content in the fermentation medium including the biomass present is preferably always below 35 g/kg, in particular below 30 g/kg, during the course of the entire fermentation process. Especially preferably, the total salt content during the entire fermentation process, with regard to the liquid fermentation medium including the biomass present, is between 10 and 35 g/kg, in particular between 12 and 30 g/kg.
According to the invention, the sulphate content in the fermentation medium including the biomass present is preferably always between 5 and 16 g/kg during the course of the entire fermentation process.
According to the invention, “sulphate content” is to be understood to mean the total content of sulphate, i.e. the content of free and bound, in particular organically bound, sulphate. It can be assumed that the majority of the sulphate present in the biomass is present as a constituent of exopolysaccharides, which are involved in the formation of the cell wall of microorganisms.
According to the invention, the sulphate content is preferably determined by ascertaining the sulphur content of the biomass obtained, since the majority of the sulphur present in the biomass can be attributed to the sulphate present. Sulphur which can be attributed to other sources can be disregarded owing to the amount of sulphate present. Thus, the amount of sulphate present can be readily ascertained from the amount of sulphur ascertained.
In this connection, the sulphur content of the biomass is preferably determined by elemental analysis in accordance with DIN EN ISO 11885. For the analysis of the sulphur content of the biomass, appropriate aliquots of sample are disrupted preferably with nitric acid and hydrogen peroxide at 240° C. under pressure prior to the analysis in order to ensure the free accessibility of the sulphur present.
For the production of the feedstuff, it is therefore preferable according to the invention to use a PUFA-containing biomass which is distinguished by the fact that a sulphur content of 8 to 20 g/kg, based on the dry mass, can be detected therein by elemental analysis in accordance with DIN EN ISO 11885. In this connection, the sulphur content in the biomass is preferably 8 to 17 g/kg, in particular 8 to 14 g/kg, especially preferably 8 to 12 g/kg, based in each case on the dry mass.
According to the invention, the phosphorus content of biomasses used according to the invention is, with regard to the dry mass, preferably 1 to 6 g/kg, in particular 2 to 5 g/kg. The phosphorus content is preferably likewise ascertained by elemental analysis in accordance with DIN EN ISO 11885.
The cells are preferably fermented at a pH of 3 to 11, in particular 4 to 10, and preferably at a temperature of at least 20° C., in particular 20 to 40° C., especially preferably at least 30° C. A typical fermentation process takes up to approximately 100 hours.
According to the invention, the cells are preferably fermented up to a biomass density of at least 50, 60 or 70 g/l, in particular at least 80 or 90 g/l, especially preferably at least 100 g/l. In this case, the data are based on the content of dry biomass in relation to the total volume of the fermentation broth after the fermentation has ended. The content of dry biomass is determined by filtering-off of the biomass from the fermentation broth, subsequent washing with water, then complete drying—for example in a microwave—and lastly ascertainment of the dry weight.
After the fermentation has ended, the biomass is harvested. After harvesting the biomass or optionally even shortly before harvesting the biomass, the cells are preferably pasteurized in order to kill the cells and to inactivate enzymes which might promote lipid degradation. The pasteurization is preferably effected by heating the biomass to a temperature of 50 to 121° C. for a period of 5 to 60 minutes.
Likewise, after harvesting the biomass or optionally even shortly before harvesting the biomass, antioxidants are preferably added in order to protect the material of value present in the biomass from oxidative degradation. Preferred antioxidants in this context are BHT, BHA, TBHA, ethoxyquin, beta-carotene, vitamin E and vitamin C. The antioxidant, if used, is preferably added in an amount of 0.01 to 2% by weight.
Optionally, it is then possible before the actual drying to remove a portion of the fermentation medium from the biomass and to thus increase the solid fraction. This may be carried out in particular by centrifugation, flotation, filtration, particularly ultrafiltration or microfiltration, decanting and/or solvent evaporation. In this case, solvent evaporation is preferably carried out using a rotary evaporator, a thin-film evaporator or a falling-film evaporator in a single-stage or multistage process. Alternatively, reverse osmosis, for example, is also useful for concentrating the fermentation broth.
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, particularly 10 to 50 or 15 to 45% by weight, particularly preferably 15 to 40% by weight or 20 to 40% by weight.
This means that the biomass to be dried is preferably present in the form of a suspension having the solid fraction stated above, where the suspension is preferably a fermentation broth or concentrated fermentation broth.
After the optional concentration of the fermentation broth, the biomass is then dried, preferably by spray drying, particularly nozzle spray drying, spray granulation, fluidized bed granulation, or in a drum dryer.
Alternatively, the biomass may also be subjected to the drying step directly after harvesting without prior concentration, particularly if the fermentation broth obtained already has a high solids content, preferably as stated above.
On drying the biomass, this is preferably dried to a residual moisture content of at most 10% by weight, particularly 0 to 10% by weight, particularly preferably at most 8% by weight, particularly 0.5 to 8% by weight, above all at most 6 or 5% by weight, particularly 0.5 to 6 or 0.5 to 5% by weight.
According to the invention, “dry mass” is accordingly preferably to be understood to mean a product having a moisture content of below 10% by weight, in particular below 5% by weight. A free-flowing, fine-grained or coarse-grained product, preferably a granulate, is preferably obtained by the drying process. A product having the desired particle size can optionally be obtained from the granulate obtained by sieving or dust separation.
Providing a free-flowing, fine-grained powder was obtained, this can optionally be converted into a coarse-grained, free-flowing and largely dust-free product, which can be stored, by suitable compacting or granulating processes.
Conventional organic or inorganic auxiliaries or supports such as starch, gelatin, cellulose derivatives or similar substances, which are typically used in food processing or feed processing as binding agents, gelling agents or thickeners, may optionally be used in this subsequent granulation or compacting process.
“Free-flowing” according to the invention is understood to mean a powder that can flow out unhindered from a series of glass efflux vessels having different size outflow openings, at least from the vessel having the 5 millimetre opening (Klein: Seifen, Öle, Fette, Wachse 94, 12 (1968)).
“Fine-grained” according to the invention is understood to mean a powder having a predominant fraction (>50%) of particle sizes of 20 to 100 micrometres in diameter.
“Coarse-grained” according to the invention is understood to mean a powder having a predominant fraction (>50%) of particle sizes of 100 to 2500 micrometres in diameter.
“Dust-free” according to the invention is understood to mean a powder that contains only low fractions (<10%, preferably <5%) of particle sizes below 100 micrometres.
Particle sizes are preferably determined according to the invention by laser diffraction spectrometric methods. Possible methods are described in the textbook “Teilchengrößenmessung in der Laborpraxis” [Particle size measurement in the laboratory] by R. H. Müller and R. Schuhmann, Wssenschaftliche Verlagsgesellschaft Stuttgart (1996) and in the textbook “Introduction to Particle Technology” by M. Rhodes, Wiley & Sons (1998).
Inasmuch as various methods can be used, the first-cited usable method from the textbook by R. H. Müller and R. Schuhmann for the measuring of particle size is preferably used.
The biomass obtained by drying preferably has a fraction of at least 80% by weight, particularly at least 90% by weight, particularly preferably at least 95% by weight, of particles having a particle size of 100 to 3500 micrometres, preferably 100 to 3000 micrometres, above all 100 to 2500 micrometres.
The cells were cultured for about 75 h in a feed process using a steel fermenter having a fermenter volume of 2 litres with a total starting mass of 712 g and an attained total final mass of 1.3-1.5 kg. During the process, a glucose solution (570 g/kg glucose) was metered in (fed-batch process).
The composition of the starting medium was as follows:
Medium 1: 20 g/kg glucose; 4 g/kg yeast extract; 16 g/kg sodium sulphate; 2 g/kg ammonium sulphate; 2.46 g/kg magnesium sulphate (heptahydrate); 0.45 g/kg potassium chloride; 4.5 g/kg potassium dihydrogen phosphate; 0.1 g/kg thiamine (HCl); 5 g/kg trace element solution.
The composition of the trace element solution was as follows: 35 g/kg hydrochloric acid (37%); 1.86 g/kg manganese chloride (tetrahydrate); 1.82 g/kg zinc sulphate (heptahydrate); 0.818 g/kg sodium EDTA; 0.29 g/kg boric acid; 0.24 g/kg sodium molybdate (dihydrate); 4.58 g/kg calcium chloride (dihydrate); 17.33 g/kg iron sulphate (heptahydrate); 0.15 g/kg copper chloride (dihydrate).
Culturing was carried out under the following conditions: Culture temperature 28° C.; aeration rate 0.5 vvm, stirrer speed 600-1950 rpm, control of pH in the growth phase at 4.5 using ammonia water (25% v/v). Fermentation was carried out up to a biomass density of 116 g/l.
After the culturing process, the fermentation broths were heated to 60° C. for 20 minutes in order to prevent further cellular activity.
This was followed by a two-stage drying of the biomass: Firstly, the fermentation broth was concentrated by evaporation to a dry mass of about 20% by weight. This was followed by spray drying of the concentrated fermentation broth using a Production Minor™ spray dryer (GEA NIRO) at a drying air inlet temperature of 340° C. By means of spray drying, a powder having a dry mass of more than 95% by weight was thus obtained.
The sulphate content of the biomass obtained was determined by determining the sulphur content of the biomass in accordance with DIN ISO 11885. To this end, an aliquot of the biomass was firstly disrupted under pressure at 240° C. with nitric acid and hydrogen peroxide. The sulphur content ascertained was 11 g/kg of biomass, corresponding to a sulphate content of 33 g/kg of biomass.
The feedstuff mixtures shown in Table 1 were produced. Besides the biomass to be used according to the invention as per Example 1, two further commercially available Labyrinthulea biomasses and also fish oil as a currently still customary source of omega-3 fatty acids were tested for comparison.
The feedstuff mixtures were each produced by mixing of the components—with the exception of the oils—using a double-helix mixer (model 500L, TGC Extrusion, France). The mixtures thus obtained were then comminuted to particle sizes below 250 μm using a hammer mill (model SH1, Hosokawa-Alpine, Germany).
For the extrusion process, use was made in each case of 140 kg per feedstuff. The extrusion process was carried out using a twin-screw extruder (CLEXTRAL BC45) having a screw diameter of 55.5 mm and a maximum flow rate of 90-100 kg/h. Pellets of 4.0 mm in size (diameter and length) were extruded. To this end, the extruder was equipped with a high-speed cutter in order to convert the product to the intended pellet size.
Various extrusion parameters were then tested in order to find out under what extrusion conditions it is possible to obtain an optimal oil load capacity of the extrudate obtained. In this connection, it became apparent that, surprisingly, an optimal oil load capacity can be achieved with a very low energy input. In this connection, the energy input was distinctly lower than when using fish oil. Furthermore, the optimal energy input in the case of a Thraustochytrium biomass to be preferably used according to the invention was again distinctly lower than in the case of commercially available Thraustochytrium biomasses. The results are shown in Table 2.
In this connection, the variable “SME” is the specific mechanical energy. This is calculated as follows:
where
U: operating voltage of the motor (here 460 V)
I: current of the motor (A)
cos ϕ: theoretical performance of the extruder motor (here 0.95)
Test SS: test speed (rpm) of the rotating screws
Max SS: maximum speed (267 rpm) of the rotating screws
QS: inlet flow rate of the mash (kg/h)
After extrusion, the extrudate was dried in a vibrating fluidized bed dryer (model DR100, TGC Extrusion, France).
This was followed, after the extrudate had cooled down, by oil coating by means of vacuum coating (vacuum coater PG-10VCLAB, Dinnisen, the Netherlands).
Abrasion resistance was ascertained as follows: Before being loaded with oil, the dried extrusion product was exposed to a mechanical load using the Holmen pellet tester (Borregaard Lignotech, Hull, UK). Before carrying out the test, the samples were screened in order to remove any adherent fine particles. The processed samples (100 g) were subsequently introduced into the pellet tester using a 2.5 mm filter screen. The pellets were subsequently conveyed through a pipe having right-angled pipe bends at high air velocity for 30 seconds. Subsequently, abrasion was determined by weighing. Abrasion resistance was specified as PDI (Pellet Durability Index), defined as the amount in percent of sample remaining in the filter screen. The test was carried out with three samples and then the mean was determined.
Water stability was carried out using the oil-loaded samples. The method was essentially carried out as described by Baeverfjord et al. (2006; Aquaculture 261, 1335-1345), with slight modifications. 10 g samples were introduced into metallic infusion baskets having a mesh size of 0.3 mm. The infusion baskets were subsequently introduced into a plastic trough containing water, and so the samples were completely covered with water. The trough was subsequently exposed for 30 minutes to a shake-agitation of 30 shake units per minute. Thereafter, the samples were carefully dried with blotting paper and then weighed before and after they had been subjected to oven drying at a temperature of 105° C. for 24 hours. Water stability was calculated as the difference in the dry weight of the sample before and after the incubation in water and specified in percent of the dry weight of the sample used before the incubation with water.
The results are shown in Table 3.
It can be seen that a feedstuff according to the invention has a distinctly higher abrasion resistance and water stability than feedstuffs which contain a commercially available Labyrinthulea biomass or fish oil as a source of omega-3 fatty acids.
| Number | Date | Country | Kind |
|---|---|---|---|
| 14187485 | Oct 2014 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2015/071666 | 9/22/2015 | WO |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO2016/050554 | 4/7/2016 | WO | A |
| Number | Name | Date | Kind |
|---|---|---|---|
| 2123134 | Cowgill | Jul 1938 | A |
| 2177031 | Tanner | Oct 1939 | A |
| 2513369 | Shaw | Jul 1950 | A |
| 3257737 | Thomas | Jun 1966 | A |
| 3257738 | Margittai et al. | Jun 1966 | A |
| 3437489 | Seiji et al. | Apr 1969 | A |
| 3773527 | Ruggerone | Nov 1973 | A |
| 3920815 | Harvey et al. | Nov 1975 | A |
| 4160040 | Luca et al. | Jul 1979 | A |
| 4209538 | Woodruff | Jun 1980 | A |
| 4228197 | Means | Oct 1980 | A |
| 4335150 | Hosaka et al. | Jun 1982 | A |
| 4592762 | Babu et al. | Jun 1986 | A |
| 4683139 | Cheng | Jul 1987 | A |
| 5113597 | Sylla | May 1992 | A |
| 5130242 | Barclay | Jul 1992 | A |
| 5298271 | Takashina et al. | Mar 1994 | A |
| 5340594 | Barclay | Aug 1994 | A |
| 5340742 | Barclay | Aug 1994 | A |
| 5434183 | Larsson-Backstrom | Jul 1995 | A |
| 5518918 | Barclay | May 1996 | A |
| 5567732 | Kyle et al. | Oct 1996 | A |
| 5574065 | Trimbo | Nov 1996 | A |
| 5622710 | Binder et al. | Apr 1997 | A |
| 5656319 | Barclay | Aug 1997 | A |
| 5698244 | Barclay | Dec 1997 | A |
| 5700506 | Mudahar | Dec 1997 | A |
| 5700837 | Trimbo | Dec 1997 | A |
| 5840358 | Hofler et al. | Nov 1998 | A |
| 6068874 | Grocholski | May 2000 | A |
| 6117905 | Higashiyama et al. | Sep 2000 | A |
| 6158147 | Smith et al. | Dec 2000 | A |
| 6166230 | Bijl et al. | Dec 2000 | A |
| 6248909 | Akimoto et al. | Jun 2001 | B1 |
| 6255505 | Bijl et al. | Jul 2001 | B1 |
| 6326037 | Mann et al. | Dec 2001 | B1 |
| 6372460 | Gladue et al. | Apr 2002 | B1 |
| 6410281 | Barclay | Jun 2002 | B1 |
| 6441208 | Bijl et al. | Aug 2002 | B2 |
| 6451567 | Barclay | Sep 2002 | B1 |
| 6602690 | Kawashima et al. | Aug 2003 | B2 |
| 6607900 | Bailey et al. | Aug 2003 | B2 |
| 6727373 | Bijl et al. | Apr 2004 | B2 |
| 6812009 | Gladue et al. | Nov 2004 | B2 |
| 6977167 | Barclay | Dec 2005 | B2 |
| 7067145 | Place et al. | Jun 2006 | B2 |
| 7259006 | Komazawa et al. | Aug 2007 | B2 |
| 7381558 | Barclay | Jun 2008 | B2 |
| 7470527 | Streekstra et al. | Dec 2008 | B2 |
| 7514096 | Haraldsson et al. | Apr 2009 | B2 |
| 7514244 | Tanaka et al. | Apr 2009 | B2 |
| 7579174 | Bailey et al. | Aug 2009 | B2 |
| 7709236 | Akimoto et al. | May 2010 | B2 |
| 7723386 | Akimoto et al. | May 2010 | B2 |
| 7732170 | Bailey et al. | Jun 2010 | B2 |
| 7847113 | Kawashima et al. | Dec 2010 | B2 |
| 7863026 | Komazawa et al. | Jan 2011 | B2 |
| 7910604 | Vasquez-Anon et al. | Mar 2011 | B2 |
| 7935365 | Dror et al. | May 2011 | B2 |
| 8030348 | Sampalis | Oct 2011 | B2 |
| 8052992 | Dror et al. | Nov 2011 | B2 |
| 8124384 | Bailey et al. | Feb 2012 | B2 |
| 8124385 | Bailey et al. | Feb 2012 | B2 |
| 8129172 | Barclay | Mar 2012 | B2 |
| 8143310 | Wang | Mar 2012 | B2 |
| 8163515 | Burja et al. | Apr 2012 | B2 |
| 8187846 | Bailey et al. | May 2012 | B2 |
| 8207363 | Apt et al. | Jun 2012 | B2 |
| 8216812 | Bailey et al. | Jul 2012 | B2 |
| 8217151 | Schaap et al. | Jul 2012 | B2 |
| 8232090 | Kallenmareth | Jul 2012 | B2 |
| 8236854 | Akimoto et al. | Aug 2012 | B2 |
| 8241868 | Higashiyama et al. | Aug 2012 | B2 |
| 8278351 | Sampalis | Oct 2012 | B2 |
| 8288133 | Bailey et al. | Oct 2012 | B2 |
| 8288134 | Bailey et al. | Oct 2012 | B2 |
| 8334363 | Hurd et al. | Dec 2012 | B2 |
| 8343753 | Chilton et al. | Jan 2013 | B2 |
| 8367774 | Frank | Feb 2013 | B2 |
| 8420349 | Kralovec et al. | Apr 2013 | B2 |
| 8900831 | Rusing et al. | Dec 2014 | B2 |
| 8921069 | Burja | Dec 2014 | B2 |
| 8945886 | Katano et al. | Feb 2015 | B2 |
| 8999663 | Avgousti et al. | Apr 2015 | B2 |
| 9045785 | Pfeifer et al. | Jun 2015 | B2 |
| 9072311 | Harel et al. | Jul 2015 | B2 |
| 9101151 | Kobzeff et al. | Aug 2015 | B2 |
| 9414612 | Apt et al. | Aug 2016 | B2 |
| 9493798 | Higashiyama et al. | Nov 2016 | B2 |
| 9649609 | Alt et al. | May 2017 | B2 |
| 9848623 | Bailey et al. | Dec 2017 | B2 |
| 10531679 | Rudinger et al. | Jan 2020 | B2 |
| 10619175 | Rabe | Apr 2020 | B2 |
| 10842174 | Durhuus | Nov 2020 | B2 |
| 20020110582 | Place et al. | Aug 2002 | A1 |
| 20030143659 | Bijl et al. | Jul 2003 | A1 |
| 20030170371 | Jobe | Sep 2003 | A1 |
| 20050118208 | Bewert | Jun 2005 | A1 |
| 20050129739 | Kohn et al. | Jun 2005 | A1 |
| 20050202148 | Streekstra et al. | Sep 2005 | A1 |
| 20050287263 | Mayer | Dec 2005 | A1 |
| 20060051484 | Yamaguchi et al. | Mar 2006 | A1 |
| 20060068019 | Daiziel | Mar 2006 | A1 |
| 20060094089 | Barclay | May 2006 | A1 |
| 20060127531 | Jobe | Jun 2006 | A1 |
| 20060160203 | Barclay | Jul 2006 | A1 |
| 20060188969 | Barclay | Aug 2006 | A1 |
| 20060265766 | Kyle et al. | Nov 2006 | A1 |
| 20060286205 | Fichtali et al. | Dec 2006 | A1 |
| 20070032383 | Newell | Feb 2007 | A1 |
| 20070082008 | Harel et al. | Apr 2007 | A1 |
| 20070092955 | De Laat et al. | Apr 2007 | A1 |
| 20070172540 | Neece | Jul 2007 | A1 |
| 20070243307 | Abril et al. | Oct 2007 | A1 |
| 20070244192 | Metz | Oct 2007 | A1 |
| 20070248738 | Abril et al. | Oct 2007 | A1 |
| 20070248739 | Abril et al. | Oct 2007 | A1 |
| 20080026128 | Yamaguchi et al. | Jan 2008 | A1 |
| 20080032381 | Bailey et al. | Feb 2008 | A1 |
| 20080038800 | Ruecker et al. | Feb 2008 | A1 |
| 20080096964 | Subramanian et al. | Apr 2008 | A1 |
| 20080166780 | Barclay | Jul 2008 | A1 |
| 20080199923 | Barclay | Aug 2008 | A1 |
| 20080254177 | Lin et al. | Oct 2008 | A1 |
| 20090004219 | Kallenmareth | Jan 2009 | A1 |
| 20090053342 | Streekstra et al. | Feb 2009 | A1 |
| 20090064567 | Lippmeier et al. | Mar 2009 | A1 |
| 20090136637 | Janssen et al. | May 2009 | A1 |
| 20090162892 | Pompejus et al. | Jun 2009 | A1 |
| 20090182050 | Barrow et al. | Jul 2009 | A1 |
| 20090202672 | Hartnell | Aug 2009 | A1 |
| 20090226571 | Freyer | Sep 2009 | A1 |
| 20090263889 | Wumpelmann | Oct 2009 | A1 |
| 20090274817 | Yamaguchi et al. | Nov 2009 | A1 |
| 20090285969 | Schaap et al. | Nov 2009 | A1 |
| 20100010088 | Chilton et al. | Jan 2010 | A1 |
| 20100086638 | Kyle et al. | Apr 2010 | A1 |
| 20100151112 | Franklin et al. | Jun 2010 | A1 |
| 20100159583 | Onose | Jun 2010 | A1 |
| 20100239712 | Brooks et al. | Sep 2010 | A1 |
| 20100266681 | Holmeide | Oct 2010 | A1 |
| 20100285105 | Radianingtyas | Nov 2010 | A1 |
| 20100297292 | Brooks et al. | Nov 2010 | A1 |
| 20100297295 | Brooks et al. | Nov 2010 | A1 |
| 20100297323 | Brooks et al. | Nov 2010 | A1 |
| 20100297331 | Brooks et al. | Nov 2010 | A1 |
| 20100303961 | Brooks et al. | Dec 2010 | A1 |
| 20100303989 | Brooks et al. | Dec 2010 | A1 |
| 20100303990 | Brooks et al. | Dec 2010 | A1 |
| 20110054029 | Kuhrts | Mar 2011 | A1 |
| 20110086128 | Abril et al. | Apr 2011 | A1 |
| 20110117068 | Lang et al. | May 2011 | A1 |
| 20110129884 | Luy | Jun 2011 | A1 |
| 20110166228 | Holmeide et al. | Jul 2011 | A1 |
| 20110177031 | Apt et al. | Jul 2011 | A1 |
| 20110189228 | Bayne et al. | Aug 2011 | A1 |
| 20110195448 | Lippmeier et al. | Aug 2011 | A1 |
| 20110195449 | Lippmeier et al. | Aug 2011 | A1 |
| 20110203168 | Franklin et al. | Aug 2011 | A1 |
| 20110258915 | Subhadra | Oct 2011 | A1 |
| 20110287158 | Yamaguchi et al. | Nov 2011 | A1 |
| 20120213905 | Nichols | Aug 2012 | A1 |
| 20120237578 | Lei et al. | Sep 2012 | A1 |
| 20130045226 | Avgousti et al. | Feb 2013 | A1 |
| 20130046020 | Liang et al. | Feb 2013 | A1 |
| 20130046105 | Avgousti et al. | Feb 2013 | A1 |
| 20130172590 | Pfeifer et al. | Jul 2013 | A1 |
| 20130302470 | Becker et al. | Nov 2013 | A1 |
| 20130344546 | Burja | Dec 2013 | A1 |
| 20140017742 | Streekstra et al. | Jan 2014 | A1 |
| 20150044356 | Bootsma et al. | Feb 2015 | A1 |
| 20150223492 | Pfeifer et al. | Aug 2015 | A1 |
| 20160066600 | Barrows | Mar 2016 | A1 |
| 20160183565 | Rudinger et al. | Jun 2016 | A1 |
| 20160227816 | Alt et al. | Aug 2016 | A1 |
| 20160249642 | Rabe et al. | Sep 2016 | A1 |
| 20160255862 | Oelmann et al. | Sep 2016 | A1 |
| 20170121742 | Aijawi et al. | May 2017 | A1 |
| 20170245523 | Pfeifer et al. | Aug 2017 | A1 |
| 20170290356 | Silva et al. | Oct 2017 | A1 |
| 20170295824 | Priefert et al. | Oct 2017 | A1 |
| 20170298318 | Rabe et al. | Oct 2017 | A1 |
| 20170303561 | Durhuus et al. | Oct 2017 | A1 |
| 20170306365 | Rabe et al. | Oct 2017 | A1 |
| 20190249108 | Cherinko et al. | Aug 2019 | A1 |
| 20190300818 | Bärz | Oct 2019 | A1 |
| 20190323043 | Diehl | Oct 2019 | A1 |
| 20200015500 | De Vriendt | Jan 2020 | A1 |
| 20200231896 | Bahl | Jul 2020 | A1 |
| 20200231898 | Bärz | Jul 2020 | A1 |
| 20200339498 | Heining | Oct 2020 | A1 |
| 20200362373 | Leininger et al. | Nov 2020 | A1 |
| 20200383353 | Wilson et al. | Dec 2020 | A1 |
| 20200404938 | Heining et al. | Dec 2020 | A1 |
| 20210017467 | Adugna et al. | Jan 2021 | A1 |
| 20210024966 | Heining et al. | Jan 2021 | A1 |
| 20210163842 | Heining et al. | Jun 2021 | A1 |
| 20210171991 | Burja et al. | Jun 2021 | A1 |
| 20210207056 | Heining et al. | Jul 2021 | A1 |
| 20210386095 | Erickson et al. | Dec 2021 | A1 |
| 20220017929 | Priefert et al. | Jan 2022 | A1 |
| 20220017930 | Priefert et al. | Jan 2022 | A1 |
| Number | Date | Country |
|---|---|---|
| 771 809 | Jun 2001 | AU |
| 646 729 | Dec 1984 | CH |
| 101 999 552 | Apr 2011 | CN |
| 102 687 810 | Sep 2012 | CN |
| 102919512 | Feb 2013 | CN |
| 103 070 293 | May 2013 | CN |
| 103 385 390 | Nov 2013 | CN |
| 10 2006 026 328 | Jan 2008 | DE |
| 1 397 410 | Jun 1975 | GB |
| 1 560 478 | Oct 1976 | GB |
| 2 324 701 | Nov 1998 | GB |
| 2 437 909 | Nov 2007 | GB |
| WO 9107498 | May 1991 | WO |
| WO 9408467 | Apr 1994 | WO |
| WO 9736996 | Oct 1997 | WO |
| WO 9737032 | Oct 1997 | WO |
| WO 9849904 | Nov 1998 | WO |
| WO-9849904 | Nov 1998 | WO |
| WO 0154510 | Aug 2001 | WO |
| WO 0200035 | Jan 2002 | WO |
| WO 2006085672 | Aug 2006 | WO |
| WO 2006124598 | Nov 2006 | WO |
| WO 2006136539 | Dec 2006 | WO |
| WO 2007074479 | Jul 2007 | WO |
| WO 2007117511 | Oct 2007 | WO |
| WO 2008019887 | Feb 2008 | WO |
| WO 2008049512 | May 2008 | WO |
| WO-2008148873 | Dec 2008 | WO |
| WO 2010090979 | Aug 2010 | WO |
| WO 2010120923 | Oct 2010 | WO |
| WO 2010128312 | Nov 2010 | WO |
| WO 2011006261 | Jan 2011 | WO |
| WO 2013022485 | Feb 2013 | WO |
| WO 2014045191 | Mar 2014 | WO |
| WO 2014122087 | Aug 2014 | WO |
| WO 2014122092 | Aug 2014 | WO |
| Entry |
|---|
| Bouvier et al., Aquafeed Twin Screw Extrusion Processing, Clextral Group, Firminy, France, 2006, p. 76-94. (Year: 2006). |
| Non Final Office Action for copending U.S. Appl. No. 15/516,044, dated Mar. 27, 2019. |
| Response to Restriction Requirement filed Jul. 5, 2019, for copending U.S. Appl. No. 15/516,023. |
| Office Action dated Aug. 6, 2019 for copending U.S. Appl. No. 15/516,023. |
| Response to Office Action filed Aug. 10, 2019 for copending U.S. Appl. No. 15/516,044. |
| Office Action dated Aug. 16, 2019 for copending U.S. Appl. No. 15/516,024. |
| Chang, K.J.L., “New Australian thraustochytrids: A Renewable Source of Biofuels, Omega-3 Oils and other Bioproducts,” Thesis; University of Tasmania; (Aug. 2013). |
| Restriction Requirement for copending U.S. Appl. No. 15/516,024, dated Mar. 4, 2019. |
| Non Final Office Action for copending U.S. Appl. No. 15/516,058, dated Mar. 12, 2019. |
| Chen, et al., “Whole cell algae powder used for increasing docosahexanoic acid content in milk of high-yielding mammal, comprises docohexanoic acid containing algae cell slurry, emulsifier, antioxidant, filler, packaging material, dispersant and water,” WPI/Thompson, Bd. 2011, Nr. 44, (Apr. 6, 2011); XP-002721747, Abstract only. |
| Uemura, “Synthesis and production of unsaturated and polyunsaturated fatty acids in yeast: current state and perspectives,” Appl. Microbiol. Biotechnol. 95:1-12 (May 2012). |
| Visentainer, et al., “Influence of diets enriched with flaxseed oil on the α-linolenic, eicosapentaenoic and docosahexaenoic fatty acid in Nile tilapia (Oreochromis niloticus),” Food Chemistry 90:557-560 (May 2005). |
| English language translation International Search Report for PCT/EP2015/071666 filed Sep. 22, 2015. |
| English language translation of the Written Opinion of the International Searching Authority for PCT/EP2015/071666 filed Sep. 22, 2015. |
| English language translation of the International Preliminary Report on Patentability for PCT/EP2015/071666 filed Sep. 22, 2015. |
| European Search Report for EP 14 18 7485 filed Oct. 2, 2014. |
| English translation of the International Search Report for PCT/EP2015/071707 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,044. |
| English language translation of the Written Opinion of the International Searching Authority for PCT/EP2015/071707 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,044. |
| English language translation of the International Preliminary Report on Patentability for PCT/EP2015/071707 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,044. |
| European Search Report with partial machine translation for EP 14 18 7479 filed Oct. 2, 2014 for copending U.S. Appl. No. 15/516,044. |
| English translation of the International Search Report for PCT/EP2015/071635 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,024. |
| English language translation of the Written Opinion of the International Searching Authority for PCT/EP2015/071635 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,024. |
| English language translation of the International Preliminary Report on Patentability for PCT/EP2015/071635 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,024. |
| European Search Report with partial machine translation for EP 14 18 7471 filed Oct. 2, 2014 for copending U.S. Appl. No. 15/516,024. |
| English translation of the International Search Report for PCT/EP2015/071689 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,023. |
| English language translation of the Written Opinion of the International Searching Authority for PCT/EP2015/071689 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,023. |
| English language translation of the International Preliminary Report on Patentability for PCT/EP2015/071689 filed Sep. 22, 2015 for copending U.S. Appl. No. 15/516,023. |
| European Search Report with partial machine translation for EP 14 18 7467 filed Oct. 2, 2014 for copending U.S. Appl. No. 15/516,023. |
| English translation of the International Search Report for PCT/EP2015/072824 filed Oct. 2, 2015 for copending U.S. Appl. No. 15/516,058. |
| English language translation of the Written Opinion of the International Searching Authority for PCT/EP2015/072824 filed Oct. 2, 2015 for copending U.S. Appl. No. 15/516,058. |
| English language translation of the International Preliminary Report on Patentability for PCT/EP2015/072824 filed Oct. 2, 2015 for copending U.S. Appl. No. 15/516,058. |
| European Search Report with partial machine translation for EP 14 18 7471 filed Oct. 2, 2014 for copending U.S. Appl. No. 15/516,058. |
| Asha, et al., “Effect of sea weed, sea grass and powdered algae in rearing the hatchery produced juveniles of Holothuria (metriatyla) scabra, jeager,” Proceedings of the National Symposium on Recent Trends in Fisheries, (2004). |
| Baeverfjord, et al., “Low feed pellet water stability and fluctuating water salinity cause separation and accumulation of dietary oil in the stomach of rainbow trout (Oncorhrynchus mykiss),” Aquaculture 261(4):1335-1345 (Dec. 2006). |
| Carter, et al., “Potential of Thraustochytrids to Partially Replace Fish Oil in Atlantic Salmon Feeds,” Marine Biotechnology 5:480-492 (Oct. 2002). |
| Hondo, et al., “Schizochytrium limacinum sp. nov., a new thraustochytrid from a mangrove area in the west Pacific Ocean,” Mycological Research 102(4):439-448 (Apr. 1998). |
| Jain, et al., “Extracellular Polysaccharide Production by Thraustochytrid Protists,” Marine Biotechnology 7:184-192 (published online May 2005). |
| Miller, et al., Replacement of fish oil with thraustochytrid Schizochytrium sp. L oil in Atlantic salmon parr (Salmo salar L) diets, Comparative Biochemistry and Physiology, Part A 148:382-392 (available online May 2007). |
| Nakahara, et al., “Production of Docosahexaenoic and Docosapentaenioc Acids by Schizochytrium sp. Isolated from Yap Islands,” Journal of American Oil Chemists' Society 73(11):1421-1425 (Nov. 1996). |
| Prabu, et al., “Effect of sodium sulphate salinity for production of docosahexaenoic acid (DHA) by Thraustochytrids aureum RAK-21,” Asian Biomedicine 6(5):693-701 (Oct. 2012). |
| Taxonomy Browser: Aurantiochytrium limacinum; taxonomy ID: 87102 (Jan. 2015). |
| XP-002721747; Database WPI Thomson Scientific, London GB; (Sep. 2013). |
| XP-002534705; Degussa: “Product Information SIPERNAT D17,” Internet citation (Sep. 2004). |
| U.S. Appl. No. 14/904,665, filed Jan. 12, 2016, US-2016/0183565, Jun. 30, 2016, Rudinger. |
| U.S. Appl. No. 15/027,429, filed Apr. 5, 2016, US-2016/0249642, Sep. 1, 2016, Rabe. |
| U.S. Appl. No. 15/516,038, filed Mar. 31, 2017, Rabe. |
| U.S. Appl. No. 15/516,023, filed Mar. 31, 2017, Silva. |
| U.S. Appl. No. 15/516,024, filed Mar. 31, 2017, Priefert. |
| U.S. Appl. No. 15/516,044, filed Mar. 31, 2017, Rabe. |
| U.S. Appl. No. 15/516,058, filed Mar. 31, 2017, Durhuus. |
| Suomalainen, et al., “The Fatty Acid Composition of Baker's and Brewer's Yeast,” Chem. Phys. Lipids 2:296-315 (1968). |
| Technicial Information 1251 (2017) http://www.sipernat.com/sites/lists/RE/DocumentsSI/TI-1251-AEROSIL-and-SIPERNAT-Silica-Versatile-Raw-Materials-for-Personal-Care-Formulations-EN.pdf download Apr. 11, 2018 (Year: 2017). |
| Response to Restriction Requirement for copending U.S. Appl. No. 15/516,024, filed May 4, 2019. |
| Restriction Requirement for copending U.S. Appl. No. 15/516,023, dated May 7, 2019. |
| Amendment and Response to Non Final Office Action for copending U.S. Appl. No. 15/516,058, filed Jun. 22, 2019. |
| Keleb, et al., “Continous twin screw extrusion for the wet granulation of lactose,” International Journal of Pharmaceutics 239:69-80 (2002). |
| Restriction Requirement for copending U.S. Appl. No. 15/516,058, dated Oct. 12, 2018. |
| Response to Restriction Requirement for copending U.S. Appl. No. 15/516,058, filed Dec. 12, 2018. |
| Amendment to accompany Response to Restriction Requirement for copending U.S. Appl. No. 15/516,058, filed Dec. 12, 2018. |
| Restriction Requirement for copending U.S. Appl. No. 15/516,044, dated Oct. 25, 2018. |
| Response to Restriction Requirement for copending U.S. Appl. No. 15/516,044, filed Dec. 25, 2018. |
| Amendment to accompany Response to Restriction Requirement for copending U.S. Appl. No. 15/516,044, filed Dec. 25, 2018. |
| Hammond, et al., “Safety Assessment of DHA-Rich Microalgae from Schizochytrium sp.,” Regulatory Toxicology and Pharmacology 33(2):192-204 (Apr. 2001). |
| Final Rejection dated Aug. 29, 2019, for copending U.S. Appl. No. 15/516,058. |
| Amendment and Response to Final Rejection filed Dec. 29, 2019, for copending U.S. Appl. No. 15/516,058. |
| Notice of Appeal filed Dec. 29, 2019, for copending U.S. Appl. No. 15/516,058. |
| Amendment and Response to Office Action filed Nov. 24, 2019, for copending U.S. Appl. No. 15/516,023. |
| Notice of Allowance dated Nov. 26, 2019, for copending U.S. Appl. No. 15/516,044. |
| Amendment Under Rule 312 filed Dec. 16, 2019, for copending U.S. Appl. No. 15/516,044. |
| Amendment and Response to Office Action filed Dec. 16, 2019, for copending U.S. Appl. No. 15/516,024. |
| Amendment & Response to Final Office Action filed Aug. 4, 2020, for copending U.S. Appl. No. 15/516,023. |
| Request for Continued Examination for copending US application filed Aug. 4, 2020, for copending U.S. Appl. No. 15/516,023. |
| Non Final Rejection dated Sep. 29, 2020, for copending U.S. Appl. No. 15/516,023. |
| Notice of Appeal filed Jul. 18, 2020, for copending U.S. Appl. No. 15/516,024. |
| Appeal Brief filed Oct. 19, 2020, for copending U.S. Appl. No. 15/516,024. |
| Leyland, et al., “Are Thraustochytrids algae?,” Fungal Biology XXX:1-6 (2017); http://dx.doi./org/10.1016/j.funbio.2017.07.006. |
| Raghukumar S., “Ecology of the marine protists, the Labyrinthulomycetes (Thraustochytrids and Labyrinthulids),” Europ. J. Protistol. 38:127-145 (2002). |
| Ratledge, C.,“ Exhibit A, Microbial production of polyunsaturated fatty acides as nutraceuticals,” Microbial Production of Food Ingredients, Enzymes and Nutraceuticals, 2 pages (2013). |
| U.S. Appl. No. 16/956,453, filed Jun. 19, 2020, US-2020/0339498 A1, Oct. 29, 2020, Heining. |
| U.S. Appl. No. 17/055,047, filed Nov. 12, 2020, Heining. |
| U.S. Appl. No. 17/055,083, filed Nov. 12, 2020, Heining. |
| Final Office Action dated Mar. 4, 2020 for copending U.S. Appl. No. 15/516,023. |
| Final Office Action dated Mar. 19, 2020 for copending U.S. Appl. No. 15/516,024. |
| Appeal Brief filed Mar. 3, 2020 for copending U.S. Appl. No. 15/516,058. |
| Advisory Action dated Apr. 6, 2020 for copending U.S. Appl. No. 15/516,058. |
| Notice of Allowance dated Jun. 4, 2020 for copending U.S. Appl. No. 15/516,058. |
| Request for Continued Examination for copending U.S. Appl. No. 15/516,058, filed Jun. 18, 2020. |
| U.S. Appl. No. 16/317,249, filed Jan. 11, 2019, US-2019/0300818 A1, Oct. 3, 2019, Bärz. |
| U.S. Appl. No. 16/317,305, filed Jan. 11, 2019, Bärz. |
| U.S. Appl. No. 16/473,805, filed Jun. 26, 2019, US-2019/0323043 A1, Oct. 24, 2019, Diehl. |
| U.S. Appl. No. 16/639,529, filed Feb. 14, 2020, Burja. |
| U.S. Appl. No. 16/644,443, filed Mar. 4, 2020, Bahl. |
| Amendment & Response to Non Final Office Action filed Jan. 29, 2021, for copending U.S. Appl. No. 15/516,023. |
| Final office Action dated Mar. 11, 2021, for copending U.S. Appl. No. 15/516,023. |
| Amendment & Response to Accompany RCE filed Jul. 12, 2021, for copending U.S. Appl. No. 15/516,023. |
| Request for Continued Examination filed Jul. 12, 2021, for copending U.S. Appl. No. 15/516,023. |
| Non Final Office Action dated Aug. 3, 2021, for copending U.S. Appl. No. 15/516,023. |
| Amendment & Response to Non Final Office Action filed Dec. 2, 2021, for copending U.S. Appl. No. 15/516,023. |
| Notice of Allowance dated Jan. 28, 2022, for copending U.S. Appl. No. 15/516,023. |
| Examiner's Answer dated Jan. 28, 2021, for copending U.S. Appl. No. 15/516,024. |
| Reply Brief filed Mar. 26, 2021, for copending U.S. Appl. No. 15/516,024. |
| U.S. Appl. No. 16/309,632, filed Dec. 13, 2018, US-2019/0249108 A1, Aug. 15, 2019, Cherinko. |
| U.S. Appl. No. 16/636,940, filed Feb. 6, 2020, US-2020/0362373 A1, Nov. 19, 2020, Leininger. |
| U.S. Appl. No. 16/886,691, filed May 28, 2020, US-2020/0383353 A1, Dec. 10, 2020, Wilson. |
| U.S. Appl. No. 16/956,820, filed Jun. 22, 2020, US-2020/0404938 A1, Dec. 31, 2020, Heining. |
| U.S. Appl. No. 17/042,788, filed Sep. 28, 2020, US-2021/0024966 A1, Jan. 28, 2021, Heining. |
| U.S. Appl. No. 17/042,791, filed Sep. 28, 2020, US-2021/0017467 A1, Jan. 21, 2021, Adugna. |
| U.S. Appl. No. 17/284,463, filed Apr. 10, 2021, US-2021/0386095 A1, Dec. 16, 2021, Erickson. |
| U.S. Appl. No. 17/291,608, filed May 6, 2021, US-2022/0017929 A1, Jan. 20, 2022, Priefert. |
| U.S. Appl. No. 17/291,610, filed May 6, 2021, US-2022/0017930 A1, Jan. 20, 2022, Priefert. |
| Number | Date | Country | |
|---|---|---|---|
| 20170295823 A1 | Oct 2017 | US |
