Patent Application
20230301316
Microbiological safety is an important requirement for food products. Conventional production and preservation processes ensure the microbiological safety, but the taste and the nutritional content are often negatively influenced by these processes. Hence, there is a continuing need for preservation processes that minimize the impact on the food's nutritional value and taste. In addition, the processes should be environmentally and economically acceptable.
Dairy products contain bioactive molecules with health promoting properties. Conventionally, the microbiological safety of dairy products such as milk is warranted by thermal pasteurization or ultra-high heat treatment (UHT). Both processes, however, result in a substantial degradation of said bioactive molecules, such as heat-sensitive vitamins and proteins.
Several dairy products are sold in powder form, obtained by spray-drying. In order to ensure microbiological safety and extended shelf life, a pasteurization step is conventionally applied before spay-drying. This spray-drying process thus involves pre-heating of the product in a pasteurizer under pasteurization conditions (at least 72° C. for at least 15 seconds), transporting the pasteurized product via a tower feeding line to the top of the spray-drying tower, and atomizing the liquid in the spray-dryer. Atomization is generally performed by a rotating disc or via nozzles. During transport to the top of the spray-drier, the product is not actively cooled and thus stays around 72° C. Cooling would negatively impact the capacity and energy input of the spray-drying process and would negatively affect the size of the spray-dried particles. In practice, this means that the product is at a temperature of at least 72° C. for a period of about a minute. Denaturation of most bioactive proteins, however, starts above 65° C., meaning that the nutritional value of the product will be negatively affected by this process.
The object of the present invention is to provide a process for the preparation of a microbiological safe powder comprising bioactive molecules naturally occurring in milk, via spray-drying, wherein denaturation of (health-promoting) bioactive molecules is minimized. In other words: the object is to provide a process wherein the time period during which the product is above the denaturation temperature of said bioactive molecules is minimized.
This object has been met by the process according to the present invention, which comprises the steps of:
This process involves the treatment of a liquid composition comprising bioactive molecules. Preferably, said bioactive molecules are bioactive molecules naturally occurring in milk.
In this specification, the term “milk” refers to milk obtained from cattle (e.g. cows, buffalos, sheep, goats, horses, and camels), but also to human milk. Hence, the “bioactive molecules that are naturally present in milk” include bioactive molecules that are naturally present in human milk and/or in milk from cattle, such as cows.
The liquid composition comprises at least one type of bioactive molecule, meaning that the liquid composition may contain other components. The bioactive molecule naturally occurring in milk that is actually present in the composition may indeed find its origin in milk, but may also have been synthetically produced or obtained from natural sources other than milk.
Examples of bioactive molecules naturally occurring in milk include various proteins, lipids, vitamins, sialic acid, nucleotides, oligosaccharides, amino acids, and taurine.
In a preferred embodiment, the liquid composition comprises proteins naturally occurring in milk. Examples of such proteins are antimicrobial factors, immunoglobulin factors, cytokines, pro-/anti-inflammatory factors, chemokines, digestive enzymes, protein hormones, transporters, glycomacropeptides, α-lactalbumin, β-lactoglobulin, bovine serum albumin, and proteins of the milk fat globule membrane. Examples of antimicrobial factors are immunoglobulins, lactoferrin, lysozyme, and antimicrobial peptides such as β-defensins and complement C3. Immunoglobulins may comprise one or more selected from IgA, IgE, IgG, IgM, and IgD. In a preferred embodiment, the liquid composition comprises IgA and/or IgG in one or more subtypes thereof.
The liquid composition may comprise, consist essentially of, or consist of whole milk, semi-skimmed milk, skimmed milk, colostrum, reduced fat milk, low fat milk, fat-free milk, casein, sweet whey, and/or acid whey.
The liquid composition is optionally pre-heated to a temperature in the range 40-65° C., preferably 50-65° C., most preferably 55-65° C., which is below the denaturation temperature of most (health promoting) bioactive molecules. Pre-heating should not result in temperatures exceeding 65° C.
This pre-heating serves to lower the electric energy input during the subsequent steps and thus to make the process more energy-efficient.
This pre-heating can be performed batch-wise or continuously in any suitable equipment. Batch-wise pre-heating can be performed in a vessel; continuous pre-heating can be performed using a heat exchanger (e.g a plate heat exchanger). The pre-heating is preferably performed continuously.
After reaching the desired pre-heating temperature, the pre-heated liquid composition is transported to the top of a spray drying tower. There is no need for holding the composition at the desired temperature for a certain time period before conducting said transport. Therefore, the entire process can be performed in a continuous manner.
If not pre-heated, the liquid composition is preferably held below 20° C., more preferably below 15° C., and most preferably below 10° C. until reaching the top of the spay-drying tower.
The tower feeding line can be a high-pressure line or can work under regular process pressure, depending on the type of spray-dryer. If the atomizer of the spray-dryer contains spraying nozzles, the pressure in said line is preferably set in the range 50-350 MPa. A rotating disc atomizer requires pressures in the range 1-5 MPa.
At the top of the spray-drying tower, the (pre-heated) liquid composition is heated using a direct electric volumetric heater that is located within the tower feeding line. During this step, the liquid composition is raised in temperature. In other words: the (pre-heated) liquid composition entering the direct electric volumetric heater with temperature T1 will leave the direct volumetric heater with a temperature T2, wherein T2>T1. Preferably, the difference in temperature of the liquid composition before entering and after leaving the direct electric volumetric heater (i.e. T2−T1) is at least 5° C., preferably at least 10° C., even more preferably at least 20° C., and most preferably at least 30° C. The temperature of the liquid composition after heating in the direct volumetric heater is preferably in the range 60-90° C., more preferably 60-80° C., and most preferably 70-75° C.
The top of the spray-drying tower is defined as a location in the vicinity of the atomizer (e.g. spraying nozzles or a rotating disc), such that the liquid composition can move from the heater to the atomizer within a short time frame, preferably less than about 40 seconds. In contrast to the use of heat-exchangers, the use of a direct volumetric heater allows very quick heating, even of high viscosity materials like infant formula.
The direct electric volumetric heater preferably operates by dielectric heating, ohmic heating (also referred to as joules heating or resistive heating), or pulsed electric field (PEF) heating.
Dielectric heating can be performed by microwave or by radio frequency heating, with frequencies of 13.56 MHz, 27.12 MHz or 40.68 MHz for radio frequency heating and 915 MHz or 2450 MHz for microwave heating. With radiofrequency heating, the heating is caused by the movement of salt ions in the solution; with microwave heating, the heating is caused by movement of both salt ions and water molecules.
Ohmic heating and PEF heating are caused by the electric resistivity of the fluid. An electric current is passed through the product and the resistance causes the product to heat up. This can be done with a direct current, an alternating current, or a pulsed current.
The use of a PEF treatment for reducing the microbial load of dairy products is disclosed in WO 2013/007620. According to that prior art procedure, the dairy product is first heated to 20-45° C., preferably 30° C., followed by a PEF treatment. After PEF treatment, the product is said to have a temperature of 64° C. or lower, most preferably 50° C. or lower. Optionally, the composition could be guided to a spray drying tower. With the present invention—which requires the direct electric volumetric heater to be located within the tower feeding line—higher temperatures can be reached without increasing bioactive molecule denaturation, thereby improving microbial safety.
The heated liquid composition is then transported—via the tower feeding line—to the atomizer(s)—i.e. nozzles or spinning disc—of a spray-dryer and sprayed to form a powder.
Legal pasteurization requires the composition to be held at ≥72° C. for at least 15 seconds for every part of the product, or equivalent as defined in the Pasteurized Milk Ordinance of the FDA. If legal pasteurization is indeed required during the process of the present invention, the residence time in the last part of the tower feeding line—i.e. between the direct electric volumetric heater and the atomizer—should be such that the time required for legal pasteurization (or equivalent) at the applied temperature is met.
In some cases legal pasteurization is not required. In these cases the direct volumetric heater can be placed at appropriate distance from the atomizer in order to achieve the desired temperature for energy efficient spray-drying and/or sufficient inactivation of micro-organisms and at the same time ensure minimum denaturation of bioactive molecules (e.g. proteins). The use of dielectric, ohmic, or PEF heating therefore allows the residence time in the last part of the tower feeding line—i.e. between the direct electric volumetric heater and the atomizer—to be less than 20 seconds, preferably less than 15 seconds, more preferably less than 10 seconds, even more preferably less than 5 seconds, even more preferably less than 2 seconds, and most preferably less than 1 second.
PEF treatment is the preferred manner of direct electric volumetric heating in step d.
Spray-drying is subsequently performed using hot air with a temperature in the range 140-300° C., preferably 150-260° C., and most preferably 170-210° C.
Any type of spray-dryer can be used, such as Single Stage, 2-Stage, Multi Stage and Filtermat® type spray dryers.
Preferred powders that can be produced using the process of the present invention are powders containing dairy products, such as milk powder (e.g. whole milk powder, semi-skimmed milk powder, skimmed milk powder, colostrum powder, reduced fat milk powder, low fat milk powder, fat-free milk powder), casein powder, whey protein concentrate or whey protein isolate powders, serum protein concentrate or serum protein isolate powders, lactoferrin powder, nutritional compositions for infants young children, and base powders for such nutritional compositions.
But also oligosaccharides like human milk oligosaccharides, galacto-oligosaccharides, and fructo-oligosaccharides, vitamins like vitamin A or vitamin D, milk fat or milk fat-based products, phospholipids, poly-unsaturated fatty acids, and probiotics can be spray-dried with the process of the present invention.
Raw milk was heated in 5 L stainless steel buckets in a water bath while agitating. The milk was heated to 45° C. prior to homogenization. Homogenization was carried out at 170 bar (first stage) and 30 bars (second stage).
This raw milk was subjected to three different processes:
The tubular heater was a double jacketed tube wound in a coil. The double jacket was flushed counter-currently with hot water to reach the desired temperature. The PEF heating device contained ohmic heating cells with a 3 chamber design, 2× [1.8×10 mm] and 1× [1.8×20 mm], The field strength for electric heating was set at 300 V/cm. The pulse duration was gradually ramped up to 1000 μs; as soon as the pulse duration was reached the frequency was increased from 0 to 125 Hz in steps of ˜20 Hz. From 100 Hz onwards small steps of ˜5 Hz were used to prevent a temperature overshoot.
The tubular cooler was a wound double jacketed tube with ice water fed co-currently in the outer tube.
The processes were run for 15 minutes, after which samples were collected. Fluid exiting the cooler was collected in sterile containers and stored on ice.
Native immunoglobulin levels (Active IgG, active IGA, and active IgM) and lactoferrin were determined by the bovine IgG, IgA, IgM and LF ELISA quantitation set as described by R. L. Valk-Weeber, T. Eshuis-de Ruiter, L. Dijkhuizen, and S. S. van Leeuwen, International Dairy Journal, Volume 110, November 2020, 104814).
This Table shows that the level of native immunoglobulins increases with decreasing heat load.
The effect of the spray-drying on the native Ig and lactoferrin levels was studied separately by feeding milk (inlet temperature: 50° C.) to a pilot spray-dryer at a pressure of 50 bar, an air inlet temperature of 170° C., and an air outlet temperature of 80° C. No loss in active IgG, IgM, and lactoferrin was detected; and only a minor loss (about 5%) in active IgA was observed.
In other words, bioactivity loss during pasteurization and spray-drying is caused by the heat load prior to spray-drying. Reducing this heat load by conducting the process in accordance with the present invention maintains large amounts of bioactives.
| Number | Date | Country | Kind |
|---|---|---|---|
| 20183450.4 | Jul 2020 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2021/067938 | 6/30/2021 | WO |
