MXPA97003665A

MXPA97003665A - Procedure for the manufacture of a food supplement for food-based animals defermentac

Info

Publication number: MXPA97003665A
Application number: MXPA/A/1997/003665A
Authority: MX
Inventors: Hofler Andreas; Schutte Rudiger; Hertz Ulrich; Klasen Claasjurgen; Alt Hanschristian; Friedrich Heinz; Morl Lothar
Original assignee: Degussa Aktiengesellschaft
Priority date: 1996-05-31
Filing date: 1997-05-19
Publication date: 1998-04-01

Abstract

The present invention relates to a process for the manufacture of a feed supplement for animals based on fermentation broth, in which the supplement contains a fermentation product and contains completely or substantially other contents of the fermentation broth, characterized by the The fact that the fermentation broth is granulated, compacted and dried in a passage in a fluidized bed while it is supplied by mechanical means in the fluidized bed, an amount of energy sufficient for the adjustment of a desired grain diameter and for a desired density of powder stacked in addition to the energy required for the production of the fluidized bed

Description

PROCEDURE FOR THE MANUFACTURE OF A FOOD SUPPLEMENT FOR ANIMALS BASED ON FERMENTATION BROTH.

FIELD OF THE INVENTION The invention relates to a process for the manufacture of an animal feed supplement based on fermentation broth, in which the supplement - contains a fermentation product and the other contents of the fermentation broth either completely or for the most part. BACKGROUND OF THE INVENTION Animal feed is supplemented with isolated amino acids corresponding to the needs of the animals. For the supplementation of feed for animals, for example with lysine-L, the lysine monohydrochloride is mostly constituted up to now. -L with a L-lysine concentration of 78%. Since lysine-L is manufactured by fermentation, it must first be separated from all the other components of the crude fermentation broth at cost-wise steps in the manufacture of the monohydrochloride, then converted into monohydrochloride, and finally it leads to crystallization. In doing so, a large number of secondary products and the reactants necessary for reconditioning as waste are originated. As a high purity of the feed supplement is not always necessary REF: 24699 and also frequently in the secondary products of the fermentation substances of active nutritive value are still contained, in the past everything has been tried to avoid the costly manufacture of non-acid aliraento-ami, especially of pure L-lysine monohydrochloride and to transfer the crude fermentation broth, into a solid animal feed at convenient costs. But all these attempts did not lead to a result - economically acceptable, The complex combination of such means has been shown as an aggravating disadvantage, since in general - they are bad to dry, therefore hygroscopic, practically not susceptible to running, they run - risk of agglomeration, and unsuitable for demanding technical processing in food mixing workshops - for animals. Above all, the fermentation products of lysine are particularly affected here. The dried sim- ples of the crude fermentation broth by spray drying led after a short storage time to a dusty, highly hygroscopic agglomerated concentrate, which in this form can not be used as animal feed. To achieve a product susceptible to runoff and stable in storage, a large number of different types of additives should be mixed in the concentrate. But in this way the amino acid content was reduced still further, in many cases already relatively low. Such a product is described, for example, in DE-OS 23 57 119, whereby -of the fermentation broth, if appropriate after extraction of the biomass, a concentrate is produced and this is promoted contiguous with Additional substances Alternately, the lysine in the concentrate can also be released by precipitation with methanol. Also the documents DD 139 205, Uor. Mikoben Sint, 111-118 (1973), CA-105 (19); 170542g, DE 30 32 618, US 4,327,118 and CS-250 851, describe such food additives for animals made with additional fermentatively promoted substances. From the documents EP 0 122 163 and US 5,133,976 a process is known according to which with the fulfillment of very special fermentation conditions a fermentation broth can be achieved which can be dried until it is a solid and stable product, but ta-well here the lysine-L content reaches only 35-48% by weight. From here it is also known that a desiccation through azeotropic distillation with paraffin oil leads to acceptable products. But this procedure is also complex and cost intensive. To this end, tetrachloromethane of toxicological risk (CS 164706) was also used. The use of an integrated fluidized bed spray dryer, it delivers a grain of pulverization in fine fragments and porous, but susceptible to - running with very low density of stacked dust and all via high hygroscopicity. When handling these products-a considerable dust load appears. A granulation conformation in the fluidized bed is also shown to be inadequate since it also requires a large amount of aggregative (in general more than 100% by weight), which is recognized with reference to document DD 268 856 In doing so, its use is essential for absorbing water from the fermentation broth, to thereby prevent the formation of groups of granules, which would adversely affect in particular the formation of granulation. Other methods for the manufacture of animal feed supplement based on fermentation broth are known from US 4,777,051, EP 0 533 039 and EP 0 615 693. US 4,777,051 discloses a process spray drying with additional drying step-connected later. Tryptophan or threonine solutions with a content of 5-95% by weight, in relation to the overall solid content, are sprayed in a first step to a semi-dry granulate with a moisture content of about 10%, Subsequently Extract the wet granulate on a conveyor belt conveyor drier with a perforated bottom and finish drying with hot air, which results in a residual of 4% by weight of remaining moisture. Therefore the drying is carried out in two stages in two different apparatuses, which as a whole is expensive. EP 0 533 039 also deals with a process for manufacturing an animal feed supplement of amino acid based of fermentation broth, with which the supplement can be obtained directly through spray drying of the fermentation broth. For this, in the case of a variant, a part of the biomass is separated from the spray drying. By means of a very neat conduction of the fermentation, that is, by keeping a fermentation broth low in residues of organic substances, it is possible to disperse the waste even without the biomass and without additional carrier materials, to obtain a manageable granulate. In the process of EO 0 533 039, the separation step of biomass is disadvantageous on the one hand, and on the other hand, the strong dependence of the spray drying process on the preceding fermentation broth is disadvantageous. That is, the spectrum in which the broth can actually be processed is comparatively short. It is also disadvantageous that a product with a relatively low stacked dust density of less than 530 kg / m and a high hygroscopicity is reached. EP 0 615 693 solves this problem again by means of a two-step drying process. It discloses a process for the manufacture of an animal feed additive under fermentation broth in which it is dried by powder the fermentation broth, after the extraction of a part of the content, until a fine grain, which has at least 70% by weight of a maximum particle size of 100%, and which is conformed this fine grain in a second stage in a granulate, which contains at least 30% by weight fine grain. In addition to the two-stage characteristic of the "granulation drying process", it is a special disadvantage in this process, the fact that the mechanical granulation by strongly cutting mixing tools with which the fine grain is preferably shaped to the granulate, only in batches, ie can not be performed continuously, It has itself shown in practice that the granulation process leads to solid agglomerations in the Eirich-intensive blender which is preferably used. Therefore, there are frequent interruptions (many times a day) of the granulation step during which the Eirish mixer must be cleaned by hand. Batch loading naturally results in undesired product deviations. The two-stage granulation drying process means high investment costs, maintenance and energy as it is complex, At the same time the two-stage procedure requires intensive use of personnel and therefore is disadvantageous, DESCRIPTION OF THE INVENTION In view of the state of the art described and discussed in the present application, it is a task of the present invention to develop a method of the type mentioned at the outset that can be used continuously and stationary in which the process should enable the simplest possible fabrication and convenient in -costs, of a product that is less hygroscopic or sticky -possible. At the same time, drying and granulation should be carried out, if possible in one step, even for relatively unpolluted fermentation broths. In addition, the method of the present invention should permit the characterization of the feed additive characteristics of the animal. simple way These tasks are solved, as well as others not indicated in detail, of a procedure of the type mentioned at the beginning, by means of the characteristics of the characterized parts of claim 1. Advantageous procedural modifications are the object of the claims subordinated to the claim 1. Measure the granulation, compaction and drying of the fermentation broth in a fluidized bed in a single pass, while transmitting a sufficient amount of energy for the adjustment of a desired grain diameter and a desired pallid powder density. and also the energy is transmitted by a mechanical means to the fluidized bed, which is required to generate the fluidized bed, is achieved among other things, continuously produce as a final product, in a single procedure step, a qranulado according to the Specification of feed additives for animals with the special use of fermentation broth concentrates, as in the case of ration of fermentation broths. That means that no aggregator is needed for the scope of the product according to the specification. However, it is not excluded to add an aggregative. Thus, common aggregators can be used, for example pearls, if the characteristics are maintained, according to the present invention. Preferably, the additional aggregates are limited to less than 10% by weight in the final product, especially they are approximately 5% by weight. According to the present invention, such agglomerates can also be used below 1%. However, it is very particularly convenient and in the context of the invention, also an objective, to totally avoid the aggregatives. It is particularly notable during the application of the process of the present invention that the drying of fluidized bed granules can be continuously used. Therefore, it is achieved very surprisingly, to avoid the two-stage characteristic of the granulation drying process according to the state of the art which makes the cleaning by hand of the Eirich intensive mixer, which is normally used for the cleaning, particularly superfluous. second step of the two-stage process (granulation step), In addition, the process according to the present invention allows, in a particularly advantageous manner, the achievement of products with high densities of stacked dust, in which the particle discharge can be carried out continuously in a classification output and the particle distribution remains constant in stationary use. The particles produced also have an excellent solidity and exhibit excellent characteristics of stacked and sliding dust thanks to their substantially round shape. The products obtained by the process according to the present invention have extremely low humidity and are not hygroscopic. Through the use of a provision as described hereinbelow, a continuous operation is possible, whereby no agiomeration can be observed on the walls or other components such as nozzle, perforated bottom, mechanical compactor, etc. a - fluidized bed granulate drying equipment. In the case of drying of fluidized-bed granules which is preferably used for carrying out the process of the present invention, it is a method for the solidification of liquids in which a fluidized bed is produced, which means that the solid particles in suspension are maintained in an air stream or inert gas directed upwards. In this state, the solid particles are separated from each other and thus are accessible from all sides for the drops - from spraying during the spraying of additional liquid into the bed, In addition, in this state, the exchange of heat and material it is intensive between the solid particles and the sas stream. The fluidized bed or particle bed that must exist at the beginning of the fluidized bed granulate drying, preferably consists of a charge of a previous path. However, it is also possible to employ a material such as a fluidized bed that moves away from the fermentation broth concentrate to be sprayed. When a suspended particle of the fluidized bed or of the particle bed respectively is touched by a drop of fermentation broth concentrate powder, the lysed product of the spray droplet is distributed to the solid bottom by dispersion. Because of the intensive exchange of heat and material with the surrounding gas stream, solidification of the liquid film takes place rapidly by drying when the starting product is treated with a solution or suspension, or by cooling when the roasted product is melted, the particle grows by dew, - dispersion and multiple solidification, it is compact and ca round. It is understood that a certain energy supply is required for the generation of the fluidized bed. This is done, as already mentioned above, generally by means of an upward inert air stream or sas, which maintains the fluidized bed or the particle bed respectively, in suspension. In the context of the present invention, it is now important that in addition to the energy required for the generation of the fluidized bed, another energy is supplied by mechanical means to the fluidized bed. By means of this supply, a process which counteracts the growth of the granulate is obviously achieved. In the stationary fluidized bed, that is, when a continuous fluidized bed is continually employed from a dried or granulated starting material, in which the feed broth is continuously sprayed and continuously drawn-a stream of granulate, a The fine dew leads to a growth of compact granulate in the form of a shell on the grains which are in the fluidized bed. Through the additional supply of mechanical energy to the fluidized bed, a slower gravure credibility or a "particle diameter leveling, respectively." With this, the processes that counteract the normal process of growth, are Desired processes that are not based on particle destruction or unhealthy growth of particles, with this - it was particularly surprising if no additional powder appeared which could be converted by agglomeration into a new germ, against abrasion destruction that can occur in each particle size class, nor does the supply of additional mechanical energy have the same effect as the particle breakage that occurs - under common conditions and can occur for example, - by particle collisions and / or other shocks of tempering during particle roar, although both abrasion and collision of particles can occur additional minister of mechanical energy, it appears in the case, according to the present invention, that the effect is not disadvantageous, which was less predictable. In a modification of the preferred process according to the present invention, it can be recognized that an additional mechanical energy causes an increase in the density of the stacked dust and a reduction in the average gravity diameter compared with a drying of the fluidized bed granulate in which does not provide additional mechanical energy. In that, as already mentioned above, both an abrasion and a particle breakage must be taken into account, however it is particularly preferred that additionally supplied mechanical energy - produces an effect in the sense of a surface treatment and compaction on the grain in conformation. This is understood, in the context of the present invention, under the surface treatment, substantially the change in particle size by abrasion. The process for manufacturing an animal feed supplement based on fermentation broth is carried out in a particularly advantageous manner by supplying additional energy by planar movable structures in the molded bed. In this case, it can be rotary blades, wings, surface-sheets, flat steel or compactors that can be used in the bed chamber, fluidized. In this case it is possible to mechanically drive the blades, blades, flat steels, compactors or the like and thus achieve a permanent fragmentation of the granulate grain so that the particles of the fluidized bed remain below a certain grain size. However, all other tools known to those skilled in the art are possible, which can, for example, be immersed directly in the fluidized bed. Thus, one can imagine the use of an endless rotating screw or strongly cutting mixing tool in which these tools also act on the grain or the granulate in the fluidized bed and produce a reciprocal effect with the particles. . In the process method according to the present invention, a compacted product is particularly advantageous than by permanent fragmentation and abrading of the granulated grain under a certain grain size. The upper grain limit is in this, a function of an energy supply related to the flow rate of solid material through, for example, the compactor, the rotating blades or the endless rotating screw. Preferably, the process of the present invention is performed so that the average particle size of the feed supplement is adjusted to values between 0.1 and 1.5 mm, preferably 95% of the particles are in the range between 0.1 and -1.5 mm in size. Furthermore, it is particularly convenient if the particle size of the animal feed supplement is adjusted so that 95% of the particles are in the range between 0.3 and 1.3 mm, in a still more preferable variant. of the process according to the present invention, it is preferred if 95% of the particles are in the range between 0.5 and 1.2 mm. As already mentioned, the process according to the present invention results, in one step, in a single additive from a fermentation broth which can be compacted, partially or completely released -of biomass, or be in the original state , a product with an excellent density of stacked dust. In this case, the density of the stacked powder of the animal feed supplement is preferably adjusted to more than 600 kg / m. In an even more convenient procedure modification, the invention is allowed to be carried out in such a way that it is adjusted in a single step, The stacked polymer density of the animal feed supplement a-3 more than 700 kg / m, Furthermore, according to the process according to the present invention, feed supplements for animals with excellent abrasion resistance are obtained. granulated. Thus, it is possible, without further ado, by means of a suitable process guide, to adjust the abrasion resistance of the feed supplement for animals to abrasion values in the range of less than 0.1% by weight. It is particularly preferred to conduct the process of the present invention so that the abrasion resistance of the animal feed supplement is adjusted to an abrasion between 0 and 0.3% by weight. The manufacture of granules with such advantages of animal feed supplements based on fermentation broth is achieved preferably with an additional mechanical energy supply per ton of granules, in the range of 8 to 20 kWh / t. It is particularly advantageous to adjust the additional supply of mechanical energy determined as specific energy supply per tonne of granulate in the sama between 10 and 16 kWh / t. As already mentioned, the feed additives for animals can be obtained according to the process according to the present invention, by spraying fermentation broths in disoosi >; - drying clones of fluidized bed granules by means of which the fermentation broth to be sprayed can be compacted, partially or completely released from biomass, or be in the original state, that is, without treatment. The fermentation broth or the concentrate that is also to be sprayed according to the present invention are obtained according to known methods. For the animal feed additive according to the present invention, such fermentation broths as base are particularly suitable which contain as a fermentation product a -remedium or an amino acid of what is preferred as a remedy, tetracycline chloride, and as an amino acid, particularly larly, lysine, threonine or tri-tocopherol. With these products, the forming granules according to the present invention can be manufactured, particularly well. This is particularly preferred, lysine-L The animal feed additives based on fermentation broth which can be obtained according to the present invention, contain in the case of an amino acid additive, for example, the following composition of -sa dry? Amino acid free of supplement 4 to 90% by weight Max proteins, 0.5 to 20% by weight Carbon acid with less than 8 • C atoms max. 13% in oeso Total sugar max. 10% by weight Greases and oils max. 6% by weight Mineral materials max. 3 to 30% by weight This product preferably contains all the contents of the fermentatbroth. Preferably, feed additives for animals according to the present inventare obtained in which the components fall within the following ranges; Proteins 10 to 16% by weight Carbon acid with less than 8 C max atoms. 8% by weight Total sugar 2 to 10% by weight Mineral materials 5 to 25% by weight Normally, the products obtained according to the present inventcontain a residual water content of approximately 0.1% by weight. To avoid a - agglomerat the asua content should not exceed 5% by weight, however, it should not exceed a maximum of 10% by weight.

The protein content is determined from the total nitrogen content minus the inorganic nitrogen content minus the nitrogen content of free amino acids and multiplicatof the value obtained by 6.25 ((total N% - inorganic N% - N aa%) x 6.25) . The total Nitrogen content is determined by disintegrat- according to Keldal (standard procedure), the inorganic nitrogen content (ammonia less contained) is determined for example, colorimatrically, volumetrically or - potentiometrically, the amino acid nitrogen content is determined free by the suanti tative determinatof the free amino acids (amino acid analyzer (aaa)) with the following calculatof the content N, As mineral materials is called the totality of all - the inorganic cat and an. The protein content in the granules obtained according to the present inventare usually between -0.5 to 20% by weight, whereby the proteins according to the present inventare also used for increasing the stability of the granulate. Therefore, a lower range of 0.5% by weight, especially favorable granulates, should be sought, they are obtained with higher contents - high protein, between 8 and 18% by weight and particularly above 10% by weight. Normally the additives obtained according to the present inventcontain a fermentatbiomass of up to 20% by weight. Higher amino acid contents can be achieved up to a maximum of -90% by weight in the dry mass, eg, during the breeze of threonine-L with Escherichia coli BK 11M B- -3996 (FR-A 2 640 640), I assumed particularly because of the relatively simple means. In the manufacture of lysine or triotophane, respectively, with derivatives of Corynebacterium glutamine or Essherichia coli K12, the content of amino-acid is generally a little lower, particularly -for tryptophan it is now typical fermentatively a maximum had 70% by weight. Preferably, the additive obtained according to the present inventhas substantially only one component as a reactant, particularly an amino acid. Such an additive can be dosed and then added - universally corresponding to its reagent content, to any animal feed or to pre-mixes. It may also be convenient for mixtures of defined animal feeds, that there are several components, particularly amino acids, in the additive in a certain proportof one another, so that the desired concentratis achieved with an additive only. The proportof these reagents can be obtained, for example, by mixing several fermentatbroths or additives or else by dosing and adding advantageously small amounts of pure reagents, for example amino acids. In additto a single reagent - or several reagents that are either properly contained or defi ned, the additive must contain the least possible additl reagents that are indefinite or not suitable for supplementat The fermentatbroths used have - • normally a solids content of 7%., 5 to 26% by weight and contain in the case of amino acids as reactant, the same from 1 to 20% by weight. Particularly advantageous in the case of amino acids are fermentation processes, in which the amino acid exists up to at least 40% by weight in the dry mass after terminating the fermentation. In addition, it is also advantageous if the limited fermentation of sugar is carried out at least at the end, but advantageously for at least 30% of the duration of the fermentation, ie the concentration of sugar which can be used in the fermentation is maintained or reduced. fermentation medium at a maximum of - 0.3% by weight. The fermentation broths are manufactured for amino acid supplements, advantageously, so that at least one microorganism producing an amino acid is cultured in a fermentation medium containing at least one carbon source, at least one source nitrogen, mineral salts and trace elements, in which the fermentation is conducted so that a thick fermentation broth with a usable sugar content of a maximum of 4 g / l and particularly with a solid content is obtained at the end. from 7.5 to 26% by weight, an amino acid content of from 1 to 20% by weight, advantageously from 4 to 10.5% by weight, and a sugar content of a maximum of 2.6% by weight, The fermentation is advantageously cultivated, under the use of suitable microorganisms so that the dry mass of the fermentation broth contains a maximum of -15% by weight of orotein and particularly, at least 40% by weight of amino acids, a maximum of 8% by weight d and carbon acid with less than 8 C atoms, a maximum of -10% in total sugar, a maximum of 5% by weight of fats and oil and a maximum of 5 to 30% in that of mineral materials. At the end of the fermentation, the usable sugar content is adjusted to a maximum of lg / 1, that is, no sugar is added, and the fermentation is interrupted when it is reached or is below it -value. To increase the amino acid content in the dry mass or to standardize the dry mass to a certain amino acid content or to reduce the protein content of the dry mass, it can be extracted, preferably after finishing the fermentation, the biomass or, Given the case, other materials, by mechanical separation methods and leaving the substantial parts of the remnant components in the fermentation broth. If a biomass is not to be separated, fermentation should be conducted advantageously so that as little biomass is produced as possible, whereby the additional aggregate materials should be spent at the end as far as possible. Such a fermentation is described, for example, in DEA 41 30 867, example 3. Advantageously, the fermentation is conducted so that at least more than 30%, preferably more than -70% of the duration of fermentation, the concentration of usable sugar in the fermentation broth is, at most, 0.3% by weight. They were used as microorganisms to produce amino acids, mutants of the species of Coryne bacteria or Brevi bacteria, preferably suitable for lysine, for example, the strain deposited and obtainable in the German collection of microorganisms under the number DSM-5715. They are used as a carbon source, preferably oligoholoside (glucose) or sucrose. A small part can also originate from sugar beet or sugar cane molasses. This part should not exceed 5% by weight of total carbon source (equal to 10% by weight of molasses in the total carbon source). For threonine and tryptophan, mutants, preferably appropriate, of the species Escherichia co li are used, for example. , for trionine or strain BK 11M B-3996 (FR-A 2 640 640). As a source of nitrogen, in addition to ammonia or ammonium sulfate, they serve as hydrolysates of materials containing proteins such as corn gluten, soybean meal or the biomass of a previous load or, for example, swelling water of corn or fish peptone, The fermentation temperature is conveniently between 30 and 40 ° C, the PH value of the fermentation medium, between 6.0 and 8.0, The duration fermentation generally has a maximum of 100 hours. After the end of fermentation, microorganisms can be killed, thermally, or by other methods, for example, by adding a mineral acid such as sulfuric acid. Then, if necessary, the biomass is separated (partially) according to procedures known as separation, decantation, a combination of separation and decanting, ultrafiltration, or microfiltration. The fermentation broth is then compacted by known methods, for example, in a thin-film evaporator or molecular evaporator for seriousness to a pre-concentrate with a solids content of -30 to 60% by weight. This pre-concentrate can then also be subjected as the fermentation broth, directly to the process of drying the fluidized caked granules according to the present invention. Whenever a standardization of the animal feed according to the present invention is desired with respect to the amino acid content, it can be carried out, for example, by the corresponding choice of the amount of remaining biomass and / or the appropriate mixture. of pre-concentrates and / or fermentation broths. Correspondingly, biomass-free or reduced-biomass broths can also be mixed with original broths for standardization. Another possibility is the addition of small amounts of aggregatives that are not objected to by the animal feed law, such as wheat bran, wheat maize flour or perlitas. The animal feed additives obtained according to the process of the present invention, ie process products, are applied for the supplementation or manufacture of an animal feed or pre-mix for animals. In the following, an arrangement is described that is specially adapted to the method according to the present invention. This is a provision for the manufacture of a food supplement for animals based on fermentation broth, which provides a fluidized bed granulate dryer with a drying chamber that is traversed by hot air from downstream, in which there is arranged, in the chamber, a gas distribution fund on which the dry product is located during the operation, in the fluidized state in a fluidized bed with which the disposition of the fact of sue in the area is arranged -from fluidized bed is arranged, at least one separately adjustable device for the supply of additional mechanical energy in the fluidized bed. The adjustable device is in a preferred configuration, a compactor operated mechanically or electrically, which is provided with surfaces, wings or blades - rotary, The adjustable device must be arranged so that it can enter into a rec Iproca with the particle surface that make up the fluidized bed. In this, it is sufficient that during the operation of the fluidized bed (subjected to air current) a contact of the particles with the adjustable device is possible. However, it is preferred that the surfaces, wings or rotating blades of the adjustable device are completely immersed in the fluidized bed. In this state, a particularly favorable specific supply of energy is achieved by means of the adjustable device. In the following, the invention is discussed in more detail in relation to the appended figures, as well as the examples of embodiments that serve for the explanation. In the Figures, a schematic sectional view of a fluidized bed granulate drying arrangement is shown in Figure 1. Figure 2, an enlarged view in section, of detail "A" of Figure 1; and Figure 3, a section of Figure 2 along line B-B. In Figure 1? reference 1 indicates the fluidized bed granulate drying arrangement. It provides a fluidized bed chamber 2, which is suitable for the reception of the particles 3 of the fluidized bed 3. In the example illustrated, the fluidized bed chamber 2 is a cylindrical drying chamber, which is a This is crossed by hot air from the bottom upwards through the perforated bottom 6. With this, on the round gas distribution bottom 6, the dry product 3 is in fluidized state in the fluidized-bed zone, which indicates in the present example, by the particles. With the number 7 is designated a nozzle of two materials, which is arranged laterally on the dryer wall. From here, the original materials (fermentation broth) are sprayed directly into the fluidized bed. With 4 is designated an adjustable sompactation device that provides a motor-propeller M as well as devices shown in-detail in Figure 2 or 3 respectively. In FIG. 1 it can be seen that the wing head 5 is completely immersed in the fluidized bed 3. A sorting tube 8 is below the perforated bottom 6 in contact with the fluidized bed chamber 2 and serves for supplying The air of sorting as well as for the lock-out of the product through the discharge lock 9. Finally, also a powder discharge is provided in the fluidized bed granulate drying arrangement 1 so that it discharges the fine dust produced together with the air from the dryer 1, they separate in an external cyclone, and are returnable to the fluidized bed via the return of dust. In FIG. 2, the detail "A" of FIG. 1, namely the wing head 5, can be better recognized. This consists of four flat steels arranged in cross-sectional shape and arranged on an axis. rotating in which the axis is connected adjustably with the Motóriso propellant M.

The illustrated arrangement is operated as follows: the compacted or raw non-compacted fermentation broth is sprayed by the nozzle of two materials in the fluidized bed in which air or another gas or gas mixture serves as a propellant. The fluidized bed is operated therein, stationary, whereby the fluidized bed must be filled with a starting material suitable for the first start of the granulator. After the fluidization of this material with hot air and the heating of the isolated drying chamber, the desired fermentation broth or the concentrate produced therefrom can be sprayed by compaction. The fluidized bed is operated stationary, which is particularly the case when a fluidized bed is operated continuously which is approximately constant and consists of original dried and granulated material with which the feed broth is continually sprayed and a stream of feed is continuously extracted. granulated via the -classification tube and the discharge lock. The fine pulverization leads to a compact and shell-like growth of the granules on the grains in the fluidised bed. In the fluidized bed, a continuous compaction of grains of grains is achieved by means of the so-presser. that the particles remain above a predetermined particle density. The upper grain limit thereof is also a function of the energy supply of the compactor related to the solid flow rate. A sorting process by means of a separate downstream air stream in the bed causes only particles having a desired grain size of approximately 500 μm to be discharged. The combination of compactor and sorter therefore results in a very broad spectrum of grain and a high density of stacked dust of the final product. The final product is cooled during brief discharge into the air stream and can then be directly bagged after a control strainer. Production of the fermentation broth and the fermentation center, 3 In a 50-m fermentation container with a bubble-agitator and ventilation system, a sterile solution of 16760 kg of the following composition is presented, Water 15600 kg Molasses 100 kg Sucrose 220 kg.

Corn swelling water 250 kg Ammonium sulfate 1 570 kg Mineral salts and trace elements 20 kg And they adjust to a pH heat of 6.9 with a solution of ammonia. 3200 kg of a vaccine culture grown in a separate container of fermentation of Corynebacterium gluctamicum are aggressed to this solution. Within 48 hours, sterile solutions of sucrose and ammonium sulphate are added and dosed at a temperature of 33 to 35 ° C. , During the total fermentation period, the value of oH is maintained between 6.5 and 7.0 by means of an ammonia solution. The ventilation regime is adjusted 0.5 to 0.7 vvm, The total means used for this , fermentation ^ 3 in the fermenter of 50 m, have the following average position.

Water 20400 ks Molasses 400 kg Sucrose 8900 kg Swelling water of corn 290 kg Ammonium sulphate 1220 kc Ammonia 2220 kg Mineral salts and trace elements 65 kg At the end of the fermentation period about 33.5t of a fermentation broth with a solids content of about 6000 kg and a L-base-L content of about 2900 kg to 3200 kg is obtained. The fermentation broth is compacted in a molecular evaporator by gravity under reduced pressure to a solid content of about 50% by weight. The spray granulation of these concentrates is described in Examples 1 to 4, For the process according to This invention can, of course, also be used with any other fermentation broth or its concentrate respectively, By way of example, they are called the fermentation broths that are described in the European patent - T ^ -EP 0 533 039 or in the European patent applications EP 0 532 867 and EP 0 615 693 respectively. Example 1; A standard fermentation concentrate according to the aforementioned standard recipe for the manufacture of Biolys 60, serves as a starting material - granulation. The concentrate has a water content of about 53%, a content of Li-sine-L base of about 24%, a sugar content of about 1%, a biomass content of about 10% and a remainder of others Secondary products-Trios for fermentation and mineral materials. In a fluidized bed granulate drying arrangement equipped with a bottom subjected to current of a diameter of approximately 400 mm and a two-wing compactor integrated in the fluidized bed with a diameter of 150 mm, 30 kg were presented of Biolys 60 granulate as starting filler. The compactor was operated with a perimeter velocity of 20 m / s. The fluidized bed was admitted with hot air of approximately 210 ° C as the drying and fluidization agent and continuously sprayed through a nozzle of two materials approximately 60. kg / h of lysine fermentation concentrate with the above composition. After about 4 to 5 hours, a steady state of operation was achieved with which a granulate with the following product parameters was continuously lowered. Parameters of a Biolys sue granulate were obtained in stationary operation. Humidity aprsx. 3% Powder density stacked 690 kg / '"3 Density of rammed mass 710 kg /' r, 3 Particle size distribution 10% < 900 jμm 50% < 1200 am 90% < 1550 ^ m Abrasion * 0.2% Resistance to breakage of particles 2.5 to 7 N * Erweka furabilator, 50 g, 20 min., 20 r.p.m. 400 um pin Example 2; A fermentation concentrate of the current production according to the aforementioned standard recipe for the manufacture of Biolys 60, serves as a starting material -of granulation, The concentrate has a water content of approximately 51%, a content of base of sine- L about 26%, a sugar content of about 1%, a biomass content of about% and a remainder of other secondary products of fermentation and mineral materials.

In a fluidized bed pellet drying arrangement equipped with a bottom subjected to a current of a diameter of approximately 400 mm and a compactor integrated in the fluidized bed with a propeller of -5.5 kW, 40 kg of granules were presented of Biolys 60 co as starting filling. The four-wing compactor-operated with a perimeter speed of 31 m / s. The power supply of the compactor in the fluidized bed was 490V7. The fluidised bed was admitted with heating air of approximately 220 ° C. as the drying and fluidizing agent and the lysine fermentation concentrate with the above composition was continuously sprayed through a nozzle of two materials. In the steady state of operation, about 37 kg / h of granulate were continuously produced and lowered -with the following product parameters. Parameters of a Biolys granulate obtained in stationary operation.

Humidity 1.0% 3 Density of stacked dust 737 kg / m 3 Density of tamped mass 756 kg / m Particle size distribution 10% - 390 or 50% - < 600 um 95% < 1120 yu Abrasion * 0.04% * Erweka furabilator, 50 g, 20 min, 20 r.p.m. um 45-pin. Example 3. A fermentation concentrate of the current production according to the aforementioned standard recipe for the manufacture of Biolys 60, serves as a starting material -of granulation. The concentrate has a water content of about 54%, an L-sine base content of about 24%, a sugar content of about 1%, a biomass content of about 10% and a remainder of others secondary products of fermentation and mineral materials. In a fluidized bed pellet drying arrangement equipped with a bottom subjected to current of a diameter of approximately 400 mm and an integrated four-wing compactor with a perimetral velocity of 31 m / s and with the power supply of the - Pactador in the fluidized bed was 490W, the hot air arrangement of approximately 250 ßC was accepted as a drying and fluidization agent. The lysine fermentation concentrate with the aforementioned composition was sprayed continuously through a nozzle of two materials. In the steady state of production, approximately 47 kg / h of granules were continuously produced and lowered with the following product parameters, Parameters of a Biolys granulate obtained in stationary operation. Moisture 1.3% 3 Density of stacked dust 718 kg / m 3 Density of tamped mass 747 kg / m Particle size distribution 10% .830 um 50% < 1090 m Abrasion * 0.14% * Erweka Friabilizer, 50 g, 20 min, 20 r.p. . 45 u. pin Example 4: A mixture of fermentation concentrate of the current production, according to the aforementioned standard recipe for the manufacture of Biolys 6O, with sucrose, serves as granulation starting material, The centering was mixed with crystalline sucrose and the mixing so long until the sucrose was completely resolved. The concentrate has a water content of about 50%, a L-lysine base content of about 24%, a sugar content plus sucrose of about 2.7%, a biomass content of about 10% and a remainder of other secondary products of fermentation and mineral materials. In a fluidized bed granulate drying arrangement equipped with a bottom subjected to current of a diameter of approximately 400 mm and an integrated four-wing compactor with a perimeter speed of 31 m / s and with the power supply of the compactor in the bed fluidized was 490 W, the arrangement with hot air of approximately 220 ° C was accepted as drying and fluidization agent. The lysine fermentation concentrate with the aforementioned composition was continuously sprayed through a nozzle of two materials. -In the steady state of operation, approximately 38 kg / h of granulate with the following product parameters were continuously produced and locked. Parameters of a Biolys granulate obtained in stationary operation.

Moisture 1.3% 3 Density of stacked dust 725 kg / m 3 Density of tamped mass 749 kg / m Particle size distribution 10% < 420 um 50% < 640 um 90% < 1000 um Abrasion * 0.10% * Erweka fridger, 50 g.20 min., 20 r.p.m. 45 um pin. Example ? A concentrated fermentation broth according to European patent application EP 0 615 693 serves as a granulation starting material. The concentrate has a water content of approximately 53%. After the granulation, the following composition is determined: Lysine base, L 52% by weight Other amino acids at 3% by weight Proteins 9% by weight Carbon acids with less than 8 carbon atoms 7% by weight Sugar 2% by weight Fats and oils 3% by weight Mineral materials 21% by weight Water 1.3% by weight In a fluidized bed granulate drying arrangement equipped with a bottom subjected to a current of a diameter of approximately 400 m and a compactor integrated in the fluidized bed with a 5.5 k propellant, 40 kg of granulate as starting filling, The four-winged compactor was operated with a perimeter speed of 31 m / s. The power supply by means of the compactor in the fluidized bed was 490 W. The fluidized bed was admitted with hot air of approximately 220 ° C as the drying and fluidizing agent and was continuously sprayed through a two-cell bosuilla. materials, the lysine fermentation concentrate with the above composition. In the steady state of operation, approximately 35 kg / h of granulate was continuously produced and locked with the following product parameters. Parameters of a granulate of Biolys sue was obtained in stationary operation. Moisture 1.3% 3 Density of stacked dust 729 kg / m 3 Density of rammed mass 756 kg / m Particle size distribution 10% < - ^ 550 ¡u 50% < 740 or 90% 990 ra Abrasion * 0.15% Erweka furabilator, 50 g, '20 min., 20 r.p.m. 45 m pin.

It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which results from the present description of the invention. Having described the invention as above, the content of the following is claimed as property;

Claims

RE I V I N D I C C I O N E S.

1. - A process for the manufacture of a fermentation-based animal feed supplement, in which the supplement contains a fermentation product and contains completely or substantially other contents of the fermentation broth, characterized by the The fact that the fermentation broth is - granulated, compacted and dried in a passage in a fluidised bed while supplying by mechanical means in the fluidized bed, an amount of energy sufficient for - the adjustment of a desired diameter of grain and for a desired density of powder stacked in addition to the energy resisted for the production of the fluidized bed.

2. The process according to claim 1, characterized in that the additional mechanical energy effects an increase in the density of stacked dust and a reduction in the average grain diameter, compared to a bed granulate drying. fluidized in which no additional mechanical energy is supplied,

3. The method according to any of claims 1 or 2, characterized in that the additional mechanical energy supplied acts in the direction of a surface treatment v of a compaction on the Quran that is formed.

4. The method according to any of the preceding claims, characterized in that the additional energy is supplied by means of movable structures planifor is, The procedure according to claim 4, characterized in that it is they use wings, sheet surfaces or rotating flat steels in the fluidized bed chamber. 6. The method according to any of the preceding claims, characterized by -the fact of sue the average particle size of the animal feed supplement is adjusted to values between 0.1 and 1.5 mm. 7, - The method according to claim 6, characterized in that the sizes of the particles of the feed supplement for animals are adjusted so that 95% of the particles are in the range between 0.1 and 1.5 mm, 8, - The procedure according to claim 7, characterized by the fact that 95% of the particles are in the range between 0.3 and 1.2 mm, 9, - The procedure according to with any one of the preceding claims, characterized by the fact that the density of the stacked powder of the animal feed supplement is adjusted to more than 600 kg / m. 10. The process according to claim 7, characterized in that the density of stacked powder of the feed supplement 3 for animals is adjusted to more than 700 kg / m, 11, - The procedure according to any of the preceding claims, characterized in that the abrasion resistance of the animal feed supplement is adjusted to abrasion values in the range of -1.0% by weight. 12. The process according to claim 9, characterized in that the abrasion resistance of the animal feed supplement is adjusted to abrasion values between 0 and 0.3% by weight.