DE10357827A1 - Preparing enzyme granules, useful in nutritional, cleaning and pharmaceutical compositions, by spraying enzyme solution into gas stream containing solid particles, followed by drying and granulation - Google Patents

Abstract

Method for preparing enzyme granules (A) by spray drying, is new. Method for preparing enzyme granules (A) comprises: (a) spraying at least one liquid enzyme formulation into a gas stream laden with solid particles; (b) subjecting the liquid-wetted particles in the heated gas stream to drying and granulation; (c) the particles, after a residence time in the gas stream, are separated and recycled in the process volume; (d) the particles are passed to the gas inlet region; (e) fine particles, dust and particles entrained in the process gas are separated and returned to the process as seed material for granule formation; and (f) a circuit-like flow of solid is generated in the axial direction of the reaction volume by supplying material to the gas stream. An independent claim is also included for enzyme granules (A) prepared by the new method.

Description

The The invention relates to a process for the preparation of enzyme granules with the in the preamble of claim 1 mentioned features, a so available Enzyme granules with the mentioned in the preamble of claim 16 Characteristics and its use for the production of these enzyme granules containing formulations in particular according to one of claims 23 to 26 (which use at the same time part of a possible preferred variant of the manufacturing process for the enzyme granules is).

enzymes are becoming more and more prevalent in a variety of industries used. This concerns both the quantities produced and the various forms of enzymes. As a rule, enzymes are present liquid Form or as a dry substance. In the last time will be Granules as a commercial form of users or from the processing industry Industry more and more preferred. The granules are characterized by advantageous properties such as ease of dosing, very good flow properties, Homogeneous internal structure, high particle density, low dust content as well as a uniform and closed surface out. Because enzymes are usually characterized by their special properties like instability, for example in water Environment, and causation of allergenic reactions characterized can be the granule form proves to be an advantageous commercial form.

The stability Enzyme can be improved by turning it into a dry one Form are transferred. This can be done, for example, by spray-drying, various agglomeration processes (Wet granulation in mixers or fluidized bed agglomeration) or by build-up granulation in fluidized bed apparatus (spray granulation) respectively.

adversely in the spray drying is that very big Apparatus volumes needed be and the powdery Product a considerable Contains dust.

Around To reduce this dust content, the spray-drying is often by means of multi-stage drying systems executed. The disadvantage is that with enzyme granules prepared in such a multi-stage drying plant a bad, i. high roundness factor (gives the ratio of surface a granule to the surface of a perfectly round granule) of more than 1.6. Enzyme granules with a roundness factor of greater than 1.6 lead because of the small roundness and therefore existing more easily terminating protruding sections, rapidly to a high dust content in mechanical Stress, such as during packing and during transport occurs.

This Dust content requires special protective measures for the production personnel and Users as well as a significant additional expenditure on plant technology for Dedusting, venting and for recycling the dusts.

One potential Process for the preparation of enzyme granules provides the build-up granulation in the fluidized bed, as published in WO 01/83727 A2 has been. Here is a process in which the liquid enzyme formulation in a fluidized bed over Spray nozzles is injected. The dust generated in the process is separated from the exhaust air and fed back to the granulation process as a germ. The resulting granules be using one or more in the distributor plate of the Fluidized bed apparatus attached gravity funnel from the process taken. The size of the discharged Granules can be adjusted by adjusting the amount of visible gas. Optionally the granules also in addition be coated. The process uses the fluidized bed process according to EP-A-0163836 and EP-A-0332929.

Of the described fluidized bed process is characterized in that for even distribution of the process fluid needed for fluidization and drying a distributor plate over the entire cross-section of the fluidized bed apparatus is attached. The for introducing the liquid used spray nozzles spray vertically upwards and integrated directly in the distributor plate (EP-A-0332929) or be equal to the inflow base surrounded by a classifier (EP-A-0163836). The granulation germs needed for the process are made by partial spray drying the injected liquid due to partial non-overlapping (Through spraying) the spray nozzles with produced the fluidized bed material. The fluidized bed mass is by a state of equilibrium between spray-dried germs and by the sub-grain recirculated and the Granulataustrag formed. There is a separation of too large granules it not.

conditioned by introducing the liquid become the particles contained in the fluidized bed in the subject area with the liquid wets and there is a drying of the liquid film on the particle surface instead. In the remaining area of the fluidized bed is outside the nozzles no drying of particles that are essentially superficially moistened instead of. Instead, only a small proportion of in the pores the moisture contained in the particles evaporates, causing an increase the (average) particle temperature leads. A feeder of however, heated process gases are also outside the spray range the nozzles in conventional Fluidized beds necessary to mix the particles in the apparatus and constantly particles in the spraying area to transport. Since the production of enzymes is temperature sensitive, can with these known methods do not give optimal yield of enzyme activity be achieved. Besides, temperature inequalities can be distributed can not be avoided in the manufacturing process.

at this litigation in the described systems, the residence time can only be reduced be that the drying of the granules is not up to the required Final value is carried out and / or an enzyme granules of smaller grain size produced but what the quality is of the enzyme granules impaired. The known from the prior art enzyme granules have a high proportion of inactive carrier material, a high level of inactivated enzyme, a low value the mean particle size D50 (particle size, at the 50% by weight of the particles have a diameter smaller and 50% by weight the particles have a diameter larger than the mean particle size D50) or a high moisture content, or usually two or more of these Properties.

For example can according to a method described in WO 01/83727 A2 a Yield of enzyme activity of more than 85% (based on the theoretically possible total enzyme activity) only at small particles and / or a moisture content (residual moisture) of more than 5%.

The On the other hand, WO 98/55599 A2 describes a process for the preparation of enzyme granules using an extrusion apparatus and a Rondierapparates when using a carrier material (such as corn starch). This Method is also described in Example 2 of WO 01/83727.

in this connection becomes an enzyme activity yield of 95% and granules with a mean particle size D50 of 600 μm, a moisture content of 5% and a roundness factor of 1.4. This Method has the disadvantage that an enzyme preparation with 27% dry matter starch in a weight ratio of 1: 2 must be added to an extrudable mixture to reach. The obtained by the extrusion process enzyme granules thereby has a content of active enzyme material of less than 13%, based on the dry matter.

The with the spray-drying method Although according to WO 01/83727 achievable enzyme granules gives granules with a roundness factor in the preferred range of 1 to 1.6 and also with particles of average particle size D50 of 620 microns (see Table 2 experiment 2), but the content of inactive carrier material much lower, whereby the content of total enzyme is higher than that in WO 98/55599 described process product. The disadvantage, however, is in the enzyme granules according to WO 98/55599, as well as from the above Example 2 in WO 01/83727 shows that the relative proportion of active enzyme, based on the total amount of active and inactive Enzyme, at 85%, is significantly lower than in the extrusion process.

According to the procedure described in WO 01/83727, the enzyme granules are prepared by the process according to EP 0 332 929 produced. This method has the property that the bed contents are self-adjusting (see EP 0332 929 , P. 22, line 27) As a result, the residence time is no longer controllable for a given granulation performance. Thus, in Example 1, the content of the fluidized bed is 3 kg and the granulation performance is 1.5 kg / hour when granulated from an aqueous saline solution containing 23% by weight of dry matter. The residence time is fixed in this case to 2 hours. Thus, the residence time is determined there by the ratio of bed content to granulation in kg / hour.

The object of the invention is to provide a process for the preparation of enzyme granules, in particular with low dust content, in which the enzyme granules are produced continuously or batchwise with the greatest possible avoidance of temperature inequalities in the production process and increasing the yield of activity of enzymes can. At the same time, the controllability of the granulation during production should be improved. An important object of the present invention is in particular to provide a fluidized bed granulation process, which has a shorter residence time in comparison with the be knew fluidized bed processes under otherwise identical conditions, such as composition of the enzyme concentrate, drying air temperatures, average particle size D50 of the granules and roundness of the granules allows. This object is achieved by the characterizing features of claim 1, which describe a particularly gentle process beyond.

According to the invention the production of enzyme granules by a link between the thermal conditions in the spray zone and the temperature conditions Furthermore Area of the fluidized bed by means of the in claim 1 in characterizing Part features mentioned. In particular, compared to the methods of the prior art the technique achieved reduced material residence times, what to a higher one relative enzyme activity in the obtained by means of the method mentioned in claim 1 enzyme granules leads. In the process according to the invention this is achieved by supplying the heated process gas for drying mainly, i.e. in particular more than 80%, preferably exclusively in the spraying region he follows. The safe feeder of particles in the spraying area in particular takes place through the special geometric design of the apparatus using gravity, but can also be pneumatic or by combining the geometric design with use gravity and pneumatic delivery.

Of the Advantage of the solution according to the invention Claim 1 is that the production conditions to the be adapted to be produced material properties. Temperature inequalities are largely avoided, thereby also increasing the yield achieved on enzyme granules.

task Also, an enzyme granule is available to the present invention with low dust content and higher active enzyme content as in the prior art in combination with a mean grain size D50 of 60 (especially 100) microns up to 2000 μm, good storage stability, in particular a small roundness factor, and / or low moisture content.

The according to the inventive method in claim 1 and in particular the dependent claims obtainable enzyme granules after Claim 16 have these advantageous properties. These can be beneficial for the Production of all kinds of interesting formulations, in particular as in claims 23 mentioned until 26, be used, in particular by adding one or more suitable carrier materials and / or packaging in suitable forms of use.

Further advantageous embodiments are in the subclaims (the to be incorporated herein by reference), they will be largely explained in the description together with its effect.

The enzyme granules which can be prepared according to the invention are highly concentrated and water-soluble or water-dispersible and have an average particle size D50 of 60 to 2000 μm and are in particular further characterized by a dust content of <800, preferably less than 500 ppm after the hay test at a ratio of active enzyme contents to the sum active and inactive enzyme contents of 80% or greater, especially 88 or more. The compressive strength of the producible enzyme granules is advantageously 10 MPa or higher, in a possible preferred embodiment of the invention 20 to 50 MPa, and the bulk density is 500 g / l or more, in a possible preferred embodiment 550 to 850 g / l. The particle size distribution, characterized by the ratio d ₁₀ / d ₉₀ (definition: d ₁₀ is the grain diameter at which 10% of the mass of the granules are smaller than this diameter, d ₉₀ is the grain diameter at which 90% of the mass of the granules is smaller are greater than this diameter), in particular 0.4 or higher. The phytase activity of an enzyme granulate which can advantageously be prepared according to the invention (here comprising phytase as enzyme) is preferably equal to or greater than 15,000 FTU / g. One FTU is the enzyme activity which liberates 1 micromole of phosphate per minute at 37 ° C under assay conditions (0.25 M sodium acetate, pH 5.5, 51 nM sodium phytate).

The Invention will be described below with reference to a preferred embodiment explained in more detail. In the associated Drawings is schematically a plant for carrying out the inventive method shown.

The amount of heated process gas required for drying the enzyme granules to be produced 10 (usually heated air) becomes a Zuluftkammer 17 , with rectangular cross section 9 and bounding sidewalls 5 , fed. In the supply air chamber 17 the process gas is distributed 10 and passes over stomata 1 in the process room 8th in the form of gas jets 2 one. The preferably horizontal in the gap 1 entering process gas flow is through the deflection 3 preferably up into the process room 8th deflected into it and flows into the apparatus as a kind of free jet. Furthermore, the apparatus cross section may optionally be in the expansion zone 14 increase, so that the speed of the process gas flow steadily decreases towards the top. The gas leaves the apparatus as exhaust gas 11 above the expansion zone 14 over the exhaust part 19 into which an optional dedusting system (eg filter cartridges or textile filter elements) can be integrated.

In the process room 8th There is a lot of particles, which are entrained by the process gas jet upwards. In the upper area of the process room 8th as well as in the expansion zone above 14 decreases the gas velocity so that the upwardly flowing particles flow laterally out of the gas jet 23 come out and into the process room 8th fall behind. The process room 8th is at the bottom of inclined side walls 29 limited. Due to this lateral inclination, the particles are moved by gravity through the return zone 24 in the direction of the gas inlet gap 1 where they are subsequently returned from the process gas to the process room 8th be carried away.

This mechanism forms a very uniform solid circulation 15 consisting of an upward flow and a return in the direction of the process gas inlet. This results in very small amounts of particles in the process area 8th in the core zone above the deflection 3 a high particle density. In this area are one or more spray nozzles 7 arranged to spray the same direction to the process gas jet upward and serve to introduce the liquid enzyme formulation.

Due to the high particle loading in the core zone arise in the Bedüsungszone 22 very advantageous conditions for the heat and mass transfer. Furthermore, it is achieved that the liquid deposits as far as possible on the particles and these are thus wetted evenly on the particle surfaces. The uniform wetting with simultaneous high solids circulation between the spraying area and the return zone 24 causes a very uniform liquid film is formed. Through the drying process, the liquid evaporates and leaves with the exhaust gas 11 the apparatus. The solid contained in the formulation remains on the particle surface. As a result, the granules grow very uniformly and homogeneously, resulting in a very narrow particle size distribution. Through the in the process room 8th Trained circular solid flow is in the area of the spray nozzles 7 and 6 a spray drying area and subsequently a granulation area formed.

The process gas can be a part of the particles as well as fine material and dusts as solids-laden exhaust air 20 from the process room 8th deliver. For the deposition of these particles can in the exhaust part 19 optionally integrated filter system or dedusting equipment downstream of the apparatus. In the case of an integrated dedusting system 25 For example, compressed air pulses 18 be used to the retained particles as a separated solid 21 in the process room 8th due.

Compared to fluidized bed apparatuses with integrated filter systems, the dust return is facilitated by the fact that the upward process gas flow is substantially localized and thus the particles to be returned safely fall outside the gas jet. Due to the suction effect near the gas inlet gap 1 this mechanism is additionally promoted. Alternatively, particles deposited from the exhaust air or otherwise obtained enzyme-containing particles (see below) may be introduced into the process space 8th to be led back. This can be done in the lower part of the inclined side walls 29 most diverse feeders 26 be arranged. Due to the high speed of the process gas jet near the gas inlet gap 1 the fine particles are sucked in and the spraying zone 22 where they are wetted with liquid and participate in the growth process.

Optional built-in baffles 16 Support the gas jet, enhance the suction effect and improve the supply of solids in the spraying zone 22 into it. Possibly occurring agglomeration effects are minimized, since in the spraying area very high flow velocities and thus higher separation forces occur than in fluidized beds. As a result, particles are separated and grow into very spherical granules.

The flow profile of the process gas in the process room 8th furthermore, ensures that fine particles returned from the optionally integrated filter system into the process chamber do not enter the spraying zone 22 fall behind. As a result, the adhesion of fine particles and consequent agglomeration processes are prevented.

For continuous process control, the apparatus can be equipped with optionally different feeding systems 13 be equipped for solids. As a result, for example, enzyme particles can be supplied to the process, which can be obtained, for example, by comminution of, for example, (too large) granules or / and consist of too small granules, or of one or more enzyme particles or enzyme-containing starting materials in the form of sufficiently obtained sufficiently fine dusts and / or powder. Such enzyme particles or enzyme-containing starting materials (enzyme-containing intermediates) may be products of other process stages and processes (eg spray drying of enzyme solutions). The proportion of these registered enzyme-containing intermediates is in particular 1 wt .-% or more, in a possible preferred embodiment of the invention 5 to 20 wt .-%. It is also possible and may be advantageous that the enzyme particles are prepared by a separate spray-drying of an enzyme suspension. It is also possible to supply enzyme particles in a possible advantageous embodiment of the invention from the very beginning. These particles then serve as granulation nuclei or as starter filling to shorten the commissioning time. In addition, additives in solid form can be introduced into the process, which are to be embedded in the enzyme granules.

Furthermore, the apparatus with discharge organs 4 be provided to particles from the process room 8th to be able to remove. This can be done for example by an overflow or by a volumetric discharge (eg a rotary valve) or by a gravity safe (eg, an exposed gas zigzag sifter or a riser sifter).

Optionally, mechanical aggregates 27 in the process room 8th but preferably in the region of the return zone 24 be attached to the inclined walls to produce by comminution sufficient fine material as nuclei for the granulation process. Furthermore, the return zone 24 optional for the positioning of heaters or other heat transfer devices 28 be used. For example, the apparatus wall may be double-walled in order to use it, for example, using liquid or gaseous heat carriers for heating or cooling. Alternatively, microwave heaters could be used to trap the particles in the return zone 24 nachzutrocknen or preheat.

In the process room 8th or in the overlying parts of the apparatus, eg the expansion zone 14 and the exhaust part 19 , can optionally spray nozzles 6 are arranged, which preferably spray downwards, but also partially upwards. Here, too, the liquid enzyme formulation can be injected to produce, for example by spray drying in the apparatus granulation. Alternatively, over some of the sprayers 6 and 7 Additives or other components are sprayed in liquid form and thus homogeneously embedded in the granule structure. If the spray nozzles 7 the Heißgasbeaufschlagte supply air chamber 17 Optionally, the fluid-carrying parts can be used with insulation or different cooling systems 12 be provided to prevent damage to the liquid formulation.

to Reduction of water sensitivity and / or control of Water the invention produced Enzyme granules can these in a subsequent separate process by coating with a protective cover be provided.

When Another advantage of the process according to the invention is the very To name a simple construction, high reliability and noise immunity combines with very good cleanability. Thus be improved Production conditions, in particular with regard to hygiene requirements created when changing the product of biological substances.

Examples:

The Invention will become apparent from the following specific application examples without being limited in any way.

Example 1: Preparation of enzyme granules

An enzyme formulation containing, in addition to the enzyme solution, a stabilizer and binder components and having a final solids concentration of about 22 mass% was sprayed into an apparatus characterized by the structure described above. The process space is characterized by a rectangular cross-section and has a cross-sectional area above the inclined side walls of 0.15 x 0.2 = 0.03 m ² and a height of about 1 m. The supply of heated to about 140 ° C process air flow of about 180 kg / h was carried out over 2 longitudinally extending through the apparatus gas supply column. The liquid formulation was passed over a pressurized vertically upwardly spraying two sprayed into the process air jet with a mass flow of about 50g / min. The process room contained about 500g of enzyme particles. Due to the evaporation process, the process air cooled and left the device at about 45 ° C. The dedusting of the exhaust air was carried out by a cyclone downstream of the apparatus, and the separated solid was gravimetrically fed into the process space in the vicinity of the gap as a seed material. The removal of granules from the process space was carried out on the front side using a sieve. The fines separated in the classifier were pneumatically blown back into the process area. The removed granules have an unconsolidated bulk density of 800 g / l and the following particle size distribution (sieve analysis): > 400 μm: 0.8% by mass 315 ... 400 μm: 6.8 mass% 250 ... 315 μm: 15.3 mass% 160 ... 250 μm: 42.3 mass% 100 ... 160 μm: 24.9 mass% 0 ... 100 μm: 9.9 mass%

Example 2: Enzyme Granules with phytase from Aspergillus niger:

Commercially available Phytase (Natuphos 5000L, BASF, Ludwigshafen, Germany) is diafiltered with demineralized water and an ultrafilter having a pore size which the enzyme does not let it happen Preservatives and salts to remove. The enzyme is then ultrafiltered, a highly concentrated liquid enzyme preparation to obtain.

To 25% by weight of this liquid enzyme preparation with a phytase activity of 24,000 FTU / g and a dry content of 25% by weight becomes polyvinyl alcohol added as a binder. The remaining 75% by weight of the solution are spray-dried at an air inlet temperature of 180 ° C and an exhaust air temperature of 70 ° C in the apparatus mentioned in Example 1.

The spray-dried enzyme powder is collected in a dust-tight docked container. The result is an enzyme powder with a phytase activity of 90 000 FTU / g and 95% dry matter. The container with the spray-dried enzyme powder is attached to the entry system with a dust-tight coupling 13 docked. The liquid enzyme preparation is introduced with a metering pump through a spray nozzle into the process space 8th sprayed.

Liquid enzyme preparation and enzyme powder are supplied in a mass ratio of 4: 1. The inlet temperature is 120 ° C, the exhaust air temperature is 60 ° C. The result is a phytase granules having the properties shown in Table 1. The content of active and inactive phytase is determined using the in EP 0 420 356 described procedure for the characterization of Aspergillus ficuum phytase - the reference is incorporated herein by reference.

Table 1: Properties of the phytase granules according to Example 2

In summary, the following can be stated:
The invention relates to a process for the preparation of enzyme granules. The object of the invention is to provide a process for the preparation of enzyme granules, in which the enzyme granules can be prepared continuously or batchwise with the utmost avoidance of temperature inequalities in the manufacturing process and increasing the yield of enzyme activity. At the same time, the controllability of the granulation during production should be improved. Enzyme granules obtainable by the process and their use are disclosed.

According to the invention the production of enzyme granules by a link between the thermal conditions in the spray zone and the temperature conditions Furthermore Area of the fluidized bed. In the process according to the invention, this is achieved achieved that feed of the heated process gas for drying exclusively in the spraying region he follows. The safe feeder of particles in the spraying area This is done by the special geometric design of the apparatus using gravity.

Claims (26)

Process for the preparation of enzyme granules, characterized in that a. one or more liquid enzyme formulations are sprayed via sprayers mainly into a solids-laden gas jet, b. subject the liquid-wetted particles of material in the heated gas jet to a drying and granulation process, c. the particles are separated from the gas jet after a residence time and returned to the process room, d. the particles are supplied to the gas entry region, e. Fine particles, dusts and entrained by the process gas particles are deposited and returned to the process as seed material for the granulation process, f. by feeding material into the gas jet, a circular solid flow of solids lying in the axial direction of the reaction space is generated. Process for the preparation of enzyme granules in particular according to claim 1, characterized in that a. one or more liquid Enzyme formulations over sprayers be injected into a solids-laden gas jet, b. with liquid wetted material particles in the heated gas jet to a drying and undergo granulation process, c. the particles after a residence time separated from the gas jet and into the process room to be led back, d. the particles move through gravity inclined surfaces supplied to the gas inlet region become, e. Fine particles, dusts and entrained by the process gas particles are deposited and the process as seed material for be returned to the granulation process, f. through material supply in the over the preferably rotationally symmetric or elongated stomata supplied Gas jet (s) a lying in the axial direction of the reaction space circle-like Solids flow is produced. Method according to one of claims 1 or 2, in particular according to claim 2, characterized in that the enzyme granules via different Sighting devices are removed from the process room. Method according to one of claims 1 to 3, in particular according to Claim 2 or 3, characterized in that the enzyme granules have different volumetric discharge from the process room are removed. Method according to one or more of claims 1 to 4, in particular according to one of claims 2 to 4, characterized that too big or too small enzyme granules taken from the process from the good product be separated. Method according to one or more of claims 1 to 5 in particular according to one of claims 2 to 5, characterized that too small withdrawn from the process enzyme granules in the Process space are returned as seed material. Method according to one or more of claims 1 to 6, in particular according to one of claims 2 to 6, characterized that too big removed from the process enzyme granules by any Crushing unit crushed and in the process room as a seed material to be led back. Method according to one or more of claims 1 to 7, in particular according to one of claims 2 to 7, characterized that the recycled into the process space enzyme granules be thermally treated. Method according to claim 8, characterized in that that the enzyme granules recycled to the process space dried or preheated become. Method according to one or more of claims 1 to 9, in particular according to one of claims 2 to 9, characterized that the enzyme granules recycled to the process space be crushed. Method according to one or more of claims 1 to 10, in particular according to one or more of claims 2 to 10, characterized in that enzyme granules of different additives and be prepared with different mixing ratios. Method according to one or more of claims 1 to 11, characterized in that the material particles after a previous spray drying be subjected to a granulation process. Method according to one or more of claims 1 to 12, characterized in that the granulation process 1 wt .-% or more, preferably 5 to 20% by weight of powdered finished granule product obtainable according to one of the preceding claims 1 to 12, and / or otherwise obtained enzyme particles and / or one or more enzyme-containing intermediates selected from enzyme-containing powders and dusts supplied become. Method according to one or more of claims 1 to 13, characterized in that the available enzyme granules in a subsequent step coated by coating with a protective protective film become. Method according to one or more of claims 1 to 14, characterized in that the mean value of the residence time the enzymes in the heated process space less than 1.5 hours, preferably less than 0.5 hours. Enzyme granules obtainable according to one of claims 1 to 15, with a roundness factor of 1 to 1.6, a mean particle size D50 of 60 (in particular 100) to 2000 μm, characterized in that (i) when the proportion of the active enzyme in relation to to the sum of active and inactive enzyme content at more than 85 % is, the average grain size 50 in Range from 650 to 2000 microns (ii) when the proportion of the active enzyme as defined above greater than 88% is, the mean particle size D50 in Range of inclusive 470 to less than 650 microns (iii) if the proportion of the active enzyme as defined above is greater than 91%, the mean particle size is D50, including 230 to less than 470 μm and (iv) if the proportion of the active Enzyme is greater than 95%, the average particle size D50 at 60 to less than 230 μm is and the residual moisture is below 5 wt .-%. Enzyme granules according to claim 16, characterized in that the weight ratio of inactive material including inactive enzyme to active enzyme less than 7: 1, based on the dry weight, is. Enzyme granules obtainable according to one of claims 1 to 15, in particular enzyme granules according to claim 17, with a middle Particle size of 60 up to 800 μm, characterized in that the dust content after hay testing below 800, especially below 500 ppm. Enzyme granules according to any one of claims 16 to 18, characterized in that the compressive strength of the enzyme granules is the same or more than 10 MPa, preferably 20 to 50 MPa. Enzyme granules according to one of claims 16 to 19, characterized in that the particle size distribution of the enzyme granules, characterized by the ratio of d ₁₀ / d ₉₀ , is equal to or greater than 0.4. Enzyme granules according to any one of claims 16 to 20, characterized in that the bulk density of the enzyme granules equal to or greater than 500 g / l, preferably 550 to 850 g / l. Enzyme granules according to any one of claims 16 to 21, containing as enzyme phytase, characterized in that the phytase activity of the enzyme granules is equal to or greater than 15,000 FTU / mg. Use of an enzyme granulate according to one of claims 16 to 22 as an additive or sole active component in the preparation of formulations for Nutritional-, Purification or pharmaceutical purposes. Use according to claim 23 for the preparation of Feed. Use according to claim 23 for the preparation of a Food. Use according to claim 23 for the preparation of a Washing or rinsing agent.