Patent Application
20140228429
The present invention relates to a process for the production of extruded formulations (=extrudates) comprising emulsion droplets, to such formulations as well as to the use of such formulations in food, feed, personal care applications.
There are many ways to formulate fat soluble compounds. Fat soluble compounds are for example oils and vitamins. The types of formulations are depending i.e. on the use of these formulations in the final application as well as on the kind of material (ingredients) which are used.
One way to formulate fat soluble compounds are dried emulsions. The fat soluble compound is emulsified in an oil-in-water emulsion wherein the aqueous phase contains a matrix material and/or a suitable emulsifier. After drying, the fat soluble compound is embedded in the matrix material.
Known technologies for emulsification are e.g. rotor-stator-systems, high pressure homogenizers or ultrasonic devices. A major disadvantage of these technologies is that a relatively low viscosity (usually below 1 Pas) is required, leading to high amounts of water in the emulsion, which needs to be removed at the end.
Extrusion processes (and extruders) are well known in the field of formulations. They can be used for many different kinds of materials. The technology was first used in the caoutchouc (natural gum) industry. But after some time, the food and feed industry adopted this technology for their purposes as well.
The main advantages of using the extrusion technology is that high viscous solutions can be formulated and less water can be used for the dispersion, which then requires less drying. Furthermore an extrusion process can be run as a continuous process.
It can be found in the prior art that emulsions comprising fat soluble vitamins are extruded. US 2004/0201116 discloses pellets which are obtained by a combination of producing emulsions using devices like high pressure homogenizers with subsequent direct pelleting or extrusion as a second process step.
The goal of the present invention was to find a way to improve (also simplify) the production of extrudates comprising oil-in-water emulsion droplets, which comprise fat soluble compound(s), such as for example oils or vitamins.
A new way for the production of such extrudates was found. Surprisingly it was found out that when the emulsification is carried out inside the extruder, the process as well as the obtained extrudates are improved.
When the emulsification is carried out in the extruder (extrudation apparatus), this results in extrudates, wherein
Therefore the present invention relates to a process of production of an extrudate, wherein that extrudate comprises emulsion droplets, wherein these emulsion droplets comprise at least one fat soluble compound and at least one emulsifier and water, characterised in that the emulsifying process is carried out in the extruder.
As fat soluble compounds any known and useful fat soluble compounds can be used. Fat soluble compounds are compounds soluble in non-polar substances (such as ether, chloroform and oils). Examples of fat soluble compounds are i.e. oils and vitamins.
The oils can be from any origin. They can be natural, modified or synthetic. If the oils are natural they can be plant or animal oils. Suitable oils are i.e. coconut oil, corn oil, cottonseed oil, olive oil, palm oil, peanut oil, rapeseed oil, canola oil, safflower oil, sesame oil, soybean oil, sunflower oil, hazelnut oil, almond oil, cashew oil, macadamia oil, mongongo nut oil, pracaxi oil, pecan oil, pine nut oil, pistachio oil, sacha Inchi (Plukenetia volubilis) oil, walnut oil, polyunsaturated fatty acids (such as triglyceride and/or ethyl ester, (for example arachidonic acid, eicosapentaenoic acid, docosahexaenoic acid and γ-linolenic acid and/or ethyl ester) and oily nutraceuticals (such as rosemary extract, oregano extract, hop extract, and other lipophilic plant extracts).
Fat soluble vitamins such as vitamin A or its esters (for example vitamin A acetate and vitamin A palmitate), vitamin E or its esters (for example vitamin E acetate), vitamin K (phytomenadione) and vitamin D3 (cholecalciferol) are contemplated in the present invention. Such vitamins are readily available from commercial sources. Also, they may be prepared by conventional methods by a skilled person. Vitamins may be used in pure form, or in a suitable diluent such as a fat or oil.
Vitamin A and/or retinyl esters, such as e.g. retinyl palmitate and/or retinyl acetate and vitamin E or its esters (for example vitamin E acetate) are especially preferred.
Therefore a preferred embodiment of the present invention is a process as described above, wherein the fat soluble compound is at least one oil and/or at least one fat soluble vitamin.
More preferred is a process wherein one or more fat soluble compound is chosen from the group consisting of coconut oil, corn oil, cottonseed oil, olive oil, palm oil, peanut oil, rapeseed oil, canola oil, safflower oil, sesame oil, soybean oil, sunflower oil, hazelnut oil, almond oil, cashew oil, macadamia oil, mongongo nut oil, pracaxi oil, pecan oil, pine nut oil, pistachio oil, sacha Inchi (Plukenetia volubilis) oil, walnut oil, polyunsaturated fatty acids (such as triglyceride and/or ethyl ester, (for example arachidonic acid, eicosapentaenoic acid, docosahexaenoic acid and γ-linolenic acid and/or ethyl ester), oily nutraceuticals (such as rosemary extract, oregano extract, hop extract, and other lipophilic plant extracts), vitamin A or its esters (for example vitamin A acetate and vitamin A palmitate), vitamin E or its esters (for example vitamin E acetate), vitamin K (phytomenadione) and vitamin D3 (cholecalciferol).
In an especially preferred process one or more fat soluble compound is chosen from the group consisting of corn oil, vitamin A or its esters (for example vitamin A acetate and vitamin A palmitate) and vitamin E or its esters (for example vitamin E acetate).
At least one emulsifier is used in the process according to the present invention. Any commonly known and used emulsifier can be used. The emulsifier can be chosen depending on the final use of the extrudate afterwards. That means if the extrudate obtained by the process according to the present invention is used in food or feed product, the emulsifier must be food or feed grade.
Suitable emulsifiers are i.e. modified (food) starches, pectin, alginate, carrageenan, furcellaran, chitosan, maltodextrin, dextrin derivatives, celluloses and cellulose derivatives (e.g. cellulose acetate, methyl cellulose, hydroxypropyl methyl cellulose), lignosulfonate, polysaccharide gums (such as gum acacia, gum arabic, flaxseed gum, ghatti gum, tamarind gum and arabinogalactan), gelatine (bovine, fish, pork, poultry), plant proteins (such as are for example peas, soybeans, castor beans, cotton, potatoes, sweet potatoes, manioc, rapeseed, sunflowers, sesame, linseed, safflower, lentils, nuts, wheat, rice, maize, barley, rye, oats, lupin and sorghum), animal proteins including milk or whey proteins, lecithin, polyglycerol ester of fatty acids, monoglycerides of fatty acids, diglycerides of fatty acids, sorbitan ester, PG ester and sugar ester (as well as derivatives thereof).
The starches can be modified physically and chemically. Pregelatinized starches are examples of physically modified starches. Acidic modified, oxidized, cross-linked, starch esters, starch ethers and cationic starches are examples of chemically modified starches.
A preferred embodiment therefore relates to process, wherein at least one emulsifier is chosen from the group consisting of modified (food) starches, pectin, alginate, carrageenan, furcellaran, chitosan, maltodextrin, dextrin derivatives, celluloses and cellulose derivatives (e.g. cellulose acetate, methyl cellulose, hydroxypropyl methyl cellulose), lignosulfonate, polysaccharide gums (such as gum acacia, gum arabic, flaxseed gum, ghatti gum, tamarind gum and arabinogalactan), gelatine (bovine, fish, pork, poultry), plant proteins (such as are for example peas, soybeans, castor beans, cotton, potatoes, sweet potatoes, manioc, rapeseed, sunflowers, sesame, linseed, safflower, lentils, nuts, wheat, rice, maize, barley, rye, oats, lupin and sorghum), animal proteins including milk or whey proteins, lecithin, polyglycerol ester of fatty acids, monoglycerides of fatty acids, diglycerides of fatty acids, sorbitan ester, PG ester and sugar ester (as well as derivatives thereof).
Water is also used in the process according to the present invention. But as mentioned before, it is possible to run the process with a less water when compared to the usually used processes.
No organic solvent is used in the process according to the present invention.
It is also possible to add further ingredients (auxiliary agents) during the process of formulation (extrudation). Such auxiliary agents can be useful for the extrusion process and/or for the extrudate and/or for the product (or application), wherein the extrudate is used afterwards.
Such auxiliary agents are for example antioxidants (such as ascorbic acid or salts thereof, tocopherol (synthetic or natural)); butylated hydroxytoluene (BHT); butylated hydroxyanisole (BHA); propyl gallate; tert. butyl hydroxyquinoline and/or ascorbic acid esters of a fatty acid); ethoxyquin; plasticisers; stabilisers; humectants (such as glycerine, sorbitol, polyethylene glycol); protective colloids; dyes, fragrances; fillers and buffers.
These auxiliary agents are added optionally. When added then the amount of the auxiliary agents goes from 0.1 to 50 weight-% (wt.-%), based on the total weight of the extrudate.
The extrudates obtained by the process according to the present invention comprise:
All the percentages always add up to 100.
All the preferences listed above for the fat soluble compounds, the emulsifiers and the auxiliary agents also apply to the composition of the extrudate.
Preferably 5 wt.-% to 30 wt.-%, based on the total weight of the extrudate, of at least one fat soluble compound is used.
Preferably 15 wt.-% to 80 wt.-%, more preferably 30 wt.-% to 80 wt.-%, based on the total weight of the extrudate, of at least one emulsifier is used.
Preferably 1 wt.-% to 80 wt.-%, more preferably 1 wt.-% to 60 wt.-%, especially preferably 1 to 40 wt.-%, based on the total weight of the extrudate, of water is used.
Especially for the modified food starches the water content is preferably 10 wt.-% to 30 wt.-%, based on the total weight of the extrudate.
One of the advantages of the present invention is that the size distribution of the average droplet sizes of the oil-in-water emulsion inside the extrudate is narrow and monomodal. This means that the fat soluble compound is nearly homogenously distributed inside the extrudate, which allows afterwards very precise dosages. Furthermore, the process according to the present invention allows to producing very small sized droplets of the oil-in-water emulsion inside the extrudate. The average droplet size can be as small as 50 nm. Usually the droplets are smaller than 1 μm.
Preferably the average droplet size (d3,2) of the oil-in-water emulsion inside the extrudate is between 50 nm and 300 nm.
The droplet sizes are measured by using commonly known and standardized methods. Suitable methods are light scattering or laser diffraction.
More preferably the average droplet size (d3,2) of the oil-in-water emulsion inside the extrudate is between 100 nm and 200 nm.
The extrusion process is characterised in that the emulsification is carried out inside the extruder. Usually the three main ingredients (fat soluble compound and emulsifier and water) are added at different inlets of the extruder process. These inlets are arranged separated from each other. When (optionally) auxiliary agents are added, they can be added together with one or more of the main ingredients or they can also be added in a separate step.
Usually the emulsifier is added first, then the water and then the fat soluble compound is added. It is also possible that one ingredient is added through more than one inlet of the extruder at different locations. Therefore a further embodiment of the present invention relates to a process, wherein the emulsifier (or a mixture of emulsifiers) is added first, then the water and then afterwards the fat soluble compound (or a mixture of fat soluble compounds).
A preferred embodiment of the present invention relates to a process wherein the fat soluble compound is vitamin A (or a derivative). In this case vitamin A is either added
The temperature inside the extruder is usually between 20 and 220° C. Preferably the temperature of extrudate exiting the extruder is <100° C., more preferably the temperature inside the extruder is between 20 and 100° C. The total residence time for the ingredients in the extruder is usually between 1 and 400 s.
The amount of shear of the extrudation process according to the present invention is usually 200 to 80000 units.
Furthermore, it is also possible to pump inert gas through the extruder. The inert gas is usually pumped in at the entrance of the extruder. But it could also be pumped in at any stage of the extrusion process (also through several inlets at different locations). Inert gas can be helpful to protect sensible ingredients.
The extruder comprises usually one or more screw shafts on which various conveying or kneading type screw elements are mounted.
The material is transported by these elements through the extruder (optionally under pressure and elevated temperature). At the end (exit) of the extruder there can be a die through which the extruded material is pressed. Afterwards the extruded material is dried and cut (or also vice versa). The extruder can have several inlets through which the material can be added.
In the case of the present invention there are several inlets to add the emulsifier(s), the fat soluble compound(s), water and optionally the auxiliary agents.
The present invention also relates to an extrudate obtainable by a process, wherein that extrudate comprises emulsion droplets, wherein these emulsion droplets comprise at least one fat soluble compound and at least one emulsifier and water, characterised in that the emulsifying process is carried out in the extruder.
All the preferences as described above also apply for such an extrudate obtainable by the inventive process.
A further embodiment of the present invention relates to new extrudates. These inventive extrudates comprise oil-in-water emulsion droplets which have a very small average droplet size, and wherein the distribution of the droplet sizes is narrow and monomodal.
Therefore a further embodiment of the present invention relates to extrudates comprising oil-in-water emulsion droplets, wherein these emulsion droplets comprise
at least one fat soluble compound and
at least one emulsifier, and
water, and optionally
at least one auxiliary agent,
characterised in that the average particle size of the oil-in-water emulsion droplets inside the extrudate are less than 300 nm (preferably the average particle size of the oil-in-water emulsion droplets is between 100 nm and 200 nm).
The average particle size of the oil-in-water emulsion droplets are measured by laser diffraction with a Malvern Mastersizer 2000 and Hydro 2000 S sample dispersion unit. The average particle size of the oil-in-water emulsion droplets can also be determined by dynamic light scattering, e.g with a Malvern Zetasizer Nano.
Preferred extrudates according to the present invention comprise:
More preferred are extrudates comprising
The extrudates as obtained by the process as described above can be used in many fields of applications. Preferably the extrudates as disclosed and described above are used in food, feed and personal care products.
Therefore a further embodiment of the present invention relates to the use of the extrudates as disclosed and described above in food, feed and/or personal care products. It is to be mentioned that dietary supplements are part of our definition of food products.
A further embodiment of the present invention relates to food, feed or personal care products comprising at least one of the extrudates as disclosed and described above.
The following Examples serve to illustrate the invention. All percentages and parts (if not otherwise indicated) are related to the weight. The temperature is given (if not otherwise indicated) in degree Celsius.
The extrusion emulsification of corn oil in modified food starch was conducted according to the schematic process flow shown in
The modified food starch (HICAP 100® from National Starch), here serving as both the matrix and emulsifier, was gravimetrically fed (Brabender Technologie) into the first barrel of a co-rotating twin screw extruder (Thermo Fisher Scientific, HAAKE Polylab OS with PTW16/40 OS twin screw extruder). The extruder consisted of 10 (electrically heated and water-cooled) barrels and an optional die head with a screw diameter of 16 mm and a length to diameter ratio of 40. Demineralized water was injected into the second barrel. A solution of the modified food starch in water was formed in the downstream barrels set to 80° C. (Table 1). Corn oil was injected into barrel 5 and mixed with the modified food starch solution in the following barrels. The extrudate mass containing the emulsified corn oil droplets could be collected as a paste from the open die head or as strands using appropriate extruder dies. A typical extrudate composition is shown in Table 2. The extrudate temperature did not exceed 70° C.
A few hundred milligrams of the extrudate was dissolved in water under gentle stirring and the corn oil droplet size distribution was measured by laser diffraction with a Malvern Mastersizer 2000 and Hydro 2000 S sample dispersion unit. The resulting area weighted mean oil droplet diameter (d3,2) was 165 nm. The droplet size distribution was monomodal and rather narrow with the following characteristics: d10%=82 nm, d50%=206 nm and d90%=719 nm.
The extrusion emulsification of corn oil in modified food starch with an additive was conducted according to the schematic process flow shown in
A few hundred milligrams of the extrudate was dissolved in water under gentle stirring and the corn oil droplet size distribution was measured by laser diffraction with a Malvern Mastersizer 2000 and Hydro 2000 S sample dispersion unit. The resulting area weighted mean oil droplet diameter (d3,2) was 135 nm. The droplet size distribution was monomodal and rather narrow with the following characterisitics: d10%=74 nm, d50%=162 nm and d90%=398 nm.
The extrusion emulsification of corn oil in modified food starch with an auxiliary agent was conducted according to the schematic process flow shown in
A few hundred milligrams of the extrudate was dissolved in water under gentle stirring and the corn oil droplet size distribution was measured by laser diffraction with a Malvern Mastersizer 2000 and Hydro 2000 S sample dispersion unit. The resulting area weighted mean oil droplet diameter (d3,2) was 158 nm. The droplet size distribution was monomodal and rather narrow with the following characterisitics: d10%=85 nm, d50%=196 nm and d90%=441 nm. The corn oil droplet size was also determined with a Malvern Zetasizer Nano. A monomodal droplet size distribution was found with a peak maximum at 371 nm.
The extrusion emulsification of Vitamin A in modified food starch (HICAP 100® from National Starch) was conducted according to the schematic process flow shown in
The process was carried out on a Coperion ZSK30 co-rotating twin-screw extruder with a length to diameter ratio of 44 and 14 barrels. Crystalline Vitamin A acetate (from DSM Nutritional Products) was used as the lipophilic compound. The process was carried out under inert gas atmosphere to protect the sensitive compound (to hydrolysis and oxidation) by dosing N2 in barrel 1.
The modified food starch was gravimetrically fed (Colortronic C-Flex) to barrel 4 and pre-heated (at 80° C.) demineralized water was injected to barrel 5. The Vitamin A acetate was molten at 70° C. in a nitrogen atmosphere and added to the modified food starch solution in barrel 8 of the extruder. The compound was mixed into the matrix solution in the downstream barrels set to 60° C. (Table 5). The extrudate mass containing the emulsion oil droplets could be collected as a paste from the open die head or as strands using appropriate extruder dies. A typical extrudate composition is shown in Table 6. The extrudate temperature did not exceed 70° C.
A few hundred milligrams of the extrudate was dissolved in water under gentle stirring and the Vitamin A oil droplet size distribution was measured by laser diffraction with a Malvern Mastersizer 2000 and Hydro 2000 S sample dispersion unit. The resulting area weighted mean oil droplet diameter (d3,2) was 111 nm. The droplet size distribution was monomodal and rather narrow with the following characteristics: d10%=65 nm, d50%=130 nm and d90%=264 nm. The Vitamin A content in the extrudate was verified by HPLC (high-performance liquid chromatography), confirming that the compound oil component was not degraded or lost during the extrusion emulsification processing.
The extrusion emulsification of Vitamin E in lignosulfonate was conducted according to the schematic process flow shown in
The lignosulfonate was fed by a side feeder to barrel 4 and water was injected to barrel 5. Additional lignosulfonate could be added in barrel 8. The dl-α-tocopherol was injected in barrels 11 and 13 to the lignosulfonate solution in the extruder. All barrel temperatures were set to 60° C. The extrudate mass containing the emulsion oil droplets could be collected as a paste from the open die head or as strands using appropriate extruder dies. A typical extrudate composition is shown in Table 7.
A few hundred milligrams of the extrudate was dissolved in water under gentle stirring and the dl-α-tocopherol oil droplet size distribution was measured by laser diffraction with a Malvern Mastersizer 2000 and Hydro 2000 S sample dispersion unit. The resulting area weighted mean oil droplet diameter (d3,2) was 156 nm. The droplet size distribution was monomodal and rather narrow with the following characteristics: d10%=81 nm, d50%=196 nm and d90%=550 nm.
| Number | Date | Country | Kind |
|---|---|---|---|
| 1167927.0 | May 2011 | EP | regional |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP2012/059849 | 5/20/2012 | WO | 00 | 3/24/2014 |
