WO2019160922A1 - Procédé de séchage par pulvérisation de solutions de fucosyllactose et compositions de produit associées - Google Patents

Procédé de séchage par pulvérisation de solutions de fucosyllactose et compositions de produit associées Download PDF

Info

Publication number
WO2019160922A1
WO2019160922A1 PCT/US2019/017811 US2019017811W WO2019160922A1 WO 2019160922 A1 WO2019160922 A1 WO 2019160922A1 US 2019017811 W US2019017811 W US 2019017811W WO 2019160922 A1 WO2019160922 A1 WO 2019160922A1
Authority
WO
WIPO (PCT)
Prior art keywords
fucosyllactose
powder
process according
solution
bulk density
Prior art date
Application number
PCT/US2019/017811
Other languages
English (en)
Inventor
Niels DALGAARD
Original Assignee
Dupont Nutrition Biosciences Aps
E. I. Du Pont De Nemours And Company
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from EP18164250.5A external-priority patent/EP3546060A1/fr
Application filed by Dupont Nutrition Biosciences Aps, E. I. Du Pont De Nemours And Company filed Critical Dupont Nutrition Biosciences Aps
Priority to KR1020207026496A priority Critical patent/KR20210013007A/ko
Priority to JP2020566197A priority patent/JP2021514388A/ja
Priority to CN201980026156.8A priority patent/CN112020568A/zh
Priority to AU2019222670A priority patent/AU2019222670A1/en
Priority to CA3091514A priority patent/CA3091514A1/fr
Priority to US16/970,800 priority patent/US20210059282A1/en
Priority to EP19754060.2A priority patent/EP3755819A4/fr
Publication of WO2019160922A1 publication Critical patent/WO2019160922A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
    • C07H1/00—Processes for the preparation of sugar derivatives
    • A—HUMAN NECESSITIES
    • A21—BAKING; EDIBLE DOUGHS
    • A21D—TREATMENT, e.g. PRESERVATION, OF FLOUR OR DOUGH, e.g. BY ADDITION OF MATERIALS; BAKING; BAKERY PRODUCTS; PRESERVATION THEREOF
    • A21D13/00—Finished or partly finished bakery products
    • A21D13/04—Products made from materials other than rye or wheat flour
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
    • A23L33/10—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives
    • A23L33/125—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives containing carbohydrate syrups; containing sugars; containing sugar alcohols; containing starch hydrolysates
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
    • A23L33/40—Complete food formulations for specific consumer groups or specific purposes, e.g. infant formula
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
    • C07H3/00—Compounds containing only hydrogen atoms and saccharide radicals having only carbon, hydrogen, and oxygen atoms
    • C07H3/08—Deoxysugars; Unsaturated sugars; Osones
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K1/00—Glucose; Glucose-containing syrups
    • C13K1/06—Glucose; Glucose-containing syrups obtained by saccharification of starch or raw materials containing starch

Definitions

  • This specification relates to a process for preparing a dried fucosyllactose (FL) from an FL solution by spray drying.
  • This specification also relates to an FL in powder form having high bulk density, such as is obtained by the process disclosed in this specification, and to prebiotics, probiotics and foods comprising the FL.
  • HMOs human milk oligosaccharides
  • lactose serves as an energy source for infants
  • HMOs are generally indigestible but provide a variety of other physiological benefits.
  • various HMOs promote development of beneficial intestinal microorganisms (the“prebiotic” effect), block adhesion of pathogens to gut epithelial surfaces and modulate the innate immune system; and are thought to play a role in brain development and neuronal activity.
  • HMOs e.g ., 2’-FL and 3- FL
  • Some HMOs are synthesised by cultured microorganisms, such as recombinant A. coli, and then isolated from the broth of biomolecules produced by the culture through a series of purification steps.
  • the final stages of purification of 2’-FL or 3-FL typically include one or more steps directed to drying the oligosaccharide in solution to remove as much solvent as possible so as to produce a powder that is convenient to store and transport.
  • Various drying techniques have been reported in the art for sugars, including, for example, spray drying; fluid bed drying; flash drying; drying in a drum, cone, or spherical dryer; drying with an internal mill; vacuum drying; and
  • the solution is dispersed into droplets and exposed to hot gas (typically air in the case of 2’-FL and 3-FL) inside a chamber of a spray dryer.
  • hot gas typically air in the case of 2’-FL and 3-FL
  • the large surface area of the droplets causes the solvent to evaporate rapidly leaving solid powder particles.
  • the wet air is vented from the chamber and the powder collected.
  • a dense powder is typically more efficient to store and transport than a less dense powder.
  • Density of a powder is typically expressed as“loose bulk density”, which is the weight of powder that fits into a given volume when poured into that volume, and“tapped bulk density”, which is the weight of powder that fits into a given volume after it has been compacted into the volume by a defined number of standardised“taps”.
  • This specification generally provides processes for preparing a fucosyllactose (FL) by spray drying, as well as FL powder with high bulk density.
  • This specification provides, in part, a process for preparing dried FL, particularly dried 2’-FL or 3-FL.
  • the process comprises:
  • the FL solution comprises no organic solvent or less than 1% (by weight) of organic solvent.
  • the FL solution has a Brix value of from about 8 to about 75 %Brix before spray drying.
  • the FL solution is at a temperature of from about 2 to about 70°C before spray drying.
  • the spray dryer is a co-current spray dryer.
  • the spray dryer is a counter-current spray dryer.
  • the spray dryer is attached to an external fluid bed.
  • the spray dryer comprises an atomizer wheel, a rotary disk, a high pressure nozzle or a two fluid nozzle.
  • the spray dryer comprises an atomizer wheel.
  • the atomizer wheel operates at a speed of from about 10,000 to about 28,000 rpm.
  • the spray drying uses air at an inlet temperature of from about 120 to about 280°C.
  • the spray dryer has an air outlet temperature of from about 80 to about H0°C.
  • This specification also provides, in part, dried FL (particularly dried 2’-FL or 3- FL) prepared in accordance with this specification.
  • This specification also provides, in part, an FL in powder form, wherein the FL is 2’-FL or 3-FL.
  • the 2’-FL or 3-FL powder exhibits:
  • a lOOx tapped bulk density of from about 600 to about 850 g/L
  • the FL powder has a moisture content of less than about 9.0% (by weight) water. In some embodiments, the FL powder has a moisture content of from about 3.0 to about 5.0% (by weight) water. In some embodiments, the FL powder has a moisture content of less than about 2.3% (by weight) water.
  • This specification also provides, in part, an FL (particularly 2’-FL or 3-FL) prepared in accordance with this specification for use in prevention and/or treatment of a disease.
  • This specification provides, in part, a prebiotic product comprising an FL (particularly 2’-FL or 3-FL) prepared in accordance with this specification.
  • This specification also provides, in part, a process for preparing a prebiotic product.
  • the process comprises:
  • This specification also provides, in part, a process for preparing a prebiotic product.
  • the process comprises admixing an FL powder described in this specification with one or more prebiotic ingredients.
  • This specification also provides, in part, a probiotic product comprising an FL (particularly 2’-FL or 3-FL) prepared in accordance with this specification.
  • This specification also provides, in part, a process for preparing a probiotic product.
  • the process comprises:
  • This specification also provides, in part, a process for preparing a probiotic product.
  • the process comprises admixing an FL powder described in this specification with one or more probiotic ingredients.
  • This specification also provides, in part, a process for preparing a food.
  • the process comprises:
  • This specification also provides, in part, a process for preparing a food.
  • the process comprises admixing an FL powder described in this specification with one or more food ingredients.
  • This specification also provides, in part, a food comprising an FL (particularly 2’- FL or 3-FL) prepared in accordance with this specification.
  • the food comprises an infant formula.
  • Figure 1 shows 2’-FL powder prepared by the spray drying process described in
  • Figure 2 shows the solution that resulted from dissolving 28 grams of the 2’-FL powder prepared by the spray drying process described in Example 1 in 180 mL of water at 40°C.
  • Figure 3 shows the solution that resulted from dissolving the 3-FL powder prepared by the spray drying process described in Example 7 in water.
  • This specification provides a process for preparing a dried fucosyllactose (FL).
  • the process comprises feeding an FL solution comprising 2’-FL and/or 3-FL in an aqueous medium into a spray dryer, and spray drying the FL solution using the spray dryer.
  • FL The chemical structure of fucosyllactose (FL) consists of fucosylated lactose, i.e., a lactose disaccharide linked to a fucose monosaccharide unit. Lactose consists of a a- or b- glucose sub-unit and a b-galactose sub-unit linked by a b1-4 glycosidic bond. The structures of lactose and fucose are depicted below. a-fucose
  • 2’-FL and 3-FL are typically a white to ivory coloured solid that is soluble in water.
  • An“FL solution” comprises an FL dissolved in an aqueous medium.
  • An aqueous medium is a solvent comprising water.
  • the aqueous medium is pure water.
  • the medium comprises water with a trace amount of one or more organic solvents.
  • the medium comprises less than 1% (by weight) organic solvent.
  • the medium comprises less than 0.1% (by weight) organic solvent.
  • the medium comprises less than 0.01% (by weight) organic solvent.
  • the medium comprises less than 0.001% (by weight) organic solvent.
  • the medium comprises less than 0.0001% (by weight) organic solvent.
  • the FL solution is made before spray drying by dissolving in pure water FL crystals obtained from an earlier purification process. In some such
  • the FL solution comprises no organic solvent. In other embodiments, the FL solution comprises a trace amount of one or more organic solvents. In some such embodiments, the FL solution comprises less than 1% (by weight) organic solvent. In some embodiments, the FL solution comprises less than 0.1% (by weight) organic solvent. In some embodiments, the FL solution comprises less than 0.01% (by weight) organic solvent. In some embodiments, the FL solution comprises less than 0.001% (by weight) organic solvent. In some embodiments, the FL solution comprises less than 0.0001% (by weight) organic solvent. [35] In some embodiments, the FL solution has a Brix value of from about 8 to about 75 %Brix before spray drying.
  • the FL solution has a Brix value of from about 30 to about 65 %Brix before spray drying. In some embodiments, the FL solution has a Brix value of from about 50 to about 60 %Brix before spray drying. In some embodiments, the FL solution has a Brix value of about 50 %Brix before spray drying.
  • A“Brix value” indicates the sugar content of an aqueous solution.
  • a Brix value can be expressed as a percentage (%Brix) or as“degrees Brix” (°Brix). %Brix is used in this specification. Strictly, a Brix value is the percentage by weight of sucrose in a pure water solution, and so does not apply to solutions comprising other solutes and/or solvents. However, a Brix value is simple to measure, and, therefore, is commonly used in the art as an approximation of the sugar content of sugar solutions other than pure sucrose solutions.
  • the density of a solution may be measured and converted to a Brix value.
  • a digital density meter can perform this measurement and conversion automatically, or a hydrometer or pycnometer may be used.
  • the FL solution comprises 2’-FL. In some embodiments, the FL solution comprises no 3-FL. In some embodiments, the FL solution comprises no fucosyllactose other than 2’-FL.
  • the FL solution comprises 3-FL. In some embodiments, the FL solution comprises no 2’-FL. In some embodiments, the FL solution comprises no fucosyllactose other than 3-FL.
  • the FL solution comprises both 2’-FL and 3-FL.
  • the FL solution is at a temperature of from about 2 to about 70°C before spray drying. In some embodiments, the FL solution is at a temperature of from about 30 to about 60°C before spray drying. In some embodiments, the FL solution is at a temperature of from about 2 to about 30°C before spray drying. In some embodiments, the FL solution is at a temperature of about 30°C before spray drying. In some embodiments, the FL solution is at a temperature of about 20°C before spray drying. In some embodiments, the FL solution is at a temperature of from about 2 to about 5°C before spray drying. In some embodiments, the FL solution is heated or cooled to the desired temperature.
  • the FL solution is pasteurized at, for example, 60°C before being passed through a sterile filter (e.g ., 0.2 pm sterile filter) and then collected into one or more holding tanks.
  • a sterile filter e.g ., 0.2 pm sterile filter
  • the pasteurized FL solution may cool naturally (for example, to a temperature of from about 30 to about 60°C).
  • the holding tank(s) may include a heating and/or cooling jacket to maintain or adjust the
  • the temperature of the FL solution at a desired temperature may be heated or cooled using a separate heat exchanger to achieve a desired temperature.
  • the FL solution is at a temperature of from about 2 to about 70°C at the time it is fed into the spray dryer (immediately before it is dispersed into droplets in the spray dryer). In some embodiments, the FL solution is at a temperature of from about 30 to about 60°C immediately before it is dispersed into droplets in the spray dryer. In some embodiments, the FL solution is at a temperature of from about 2 to about 30°C at the time it is fed into the spray dryer. In some embodiments, the FL solution is at a temperature of about 30°C immediately before it is dispersed into droplets in the spray dryer. In some embodiments, the FL solution is at a temperature of about 20°C immediately before it is dispersed into droplets in the spray dryer. In some embodiments, the FL solution is at a temperature of from about 2 to about 5°C immediately before it is dispersed into droplets in the spray dryer.
  • Spray drying is an industrial process for drying a liquid containing dissolved or dispersed solids.
  • the liquid is dispersed into droplets and exposed to a flow of hot gas.
  • the large total surface area of the droplets means that the liquid evaporates very quickly, leaving dry solid particles that form a powder.
  • Spray drying is performed in a drying chamber of a spray dryer machine.
  • Various commercially available spray dryers may be suitable, such as, for example, a GEA Niro
  • Hot gas which is used to dry the liquid, is typically pumped through the drying chamber by means of a fan.
  • the gas used to dry an FL solution is air.
  • the air before entering the drying chamber, the air is sterilised by stepwise filtering with a pre-filter and a high efficiency particulate air (HEP A) filter.
  • HEP A high efficiency particulate air
  • a faster fan rate offers more drying energy and results in a lower moisture content of the dried product.
  • a faster fan rate also tends to be helpful for achieving a greater degree of particle separation when using, for example, a separation cyclone.
  • The“air inlet temperature” is the temperature of the air when it enters the drying chamber.
  • the air inlet temperature is from about 120 to about 280°C.
  • the air inlet temperature is from about 120 to about 2lO°C.
  • the air inlet temperature is from about 130 to about l90°C.
  • the air inlet temperature is about l80°C.
  • the air inlet temperature is from about 135 to about l60°C.
  • the air is pumped to an effective air distributor commonly on top of the drying chamber, which distributes the air in the correct pattern in the drying chamber.
  • the air throughput rate generally depends on various factors and the desired characteristics of the final dried product. For example, when atomization is achieved with atomizer wheel, a greater air throughput typically increases the moisture content and bulk density of the final powder product, reduces the retention time in the dryer, reduces the heat load of the spray-dried particles, reduces off-coloring of the product and/or reduces production costs associated with the spray-drying. For two fluid nozzle atomization, a greater air throughput rate normally produces smaller droplets from the nozzle, resulting in a decreased particle size distribution, bulk density and moisture content.
  • Moisture in the air generally equates to less vapor uptake capability. Moisture in the air also can result in humidity and stickiness of the final dried product. In some
  • the air outlet temperature is increased.
  • the air is dehumidified before being fed into the drying chamber. In some embodiments, the air is dehumidified before being heated.
  • the liquid to be dried (i.e., the FL solution) may be fed into the spray dryer using, for example, a pump.
  • the liquid before entering the drying chamber the liquid is sterilised by filtering through, for example, an in-line 0.2 pm cartridge filter element.
  • the feed rate of the solution generally depends on various factors and the desired characteristics of the final dried product. In general, a faster feed rate tends to increase the moisture content of the dried product and increases the product stickiness (particularly for hygroscopic products). Faster solution feed rates also may result in a greater atomizer droplet size because more liquid is being atomized. In some embodiments, when a faster solution feed rate is used, an increased air outlet temperature is also used.
  • the spray dryer comprises an atomization means (i.e., a mechanism that breaks up the liquid into droplets). The liquid passes through the atomization means as it enters the drying chamber.
  • the spray dryer comprises an atomizer wheel, a rotary disk, a high pressure nozzle or a two fluid nozzle.
  • the centrifugal force of an atomizer wheel or rotary disk spinning at high speed throws out the liquid in a spray as it enters the wheel or disk.
  • a high pressure nozzle creates a spray by forcing the liquid through an orifice at high pressure.
  • a two fluid nozzle creates a spray by contacting the liquid with a compressed gas.
  • the spray dryer comprises an atomizer wheel.
  • the desired rotational speed of the atomizer wheel generally depends on various other process parameters and the desired characteristics of the final dried product. For example, variation of the atomizer speed can typically be used as a way to control the moisture content, bulk density and particle size distribution in the final dried product. In general, slower atomizer speeds result in a product with a greater moisture content, greater bulk density and greater particle size distribution relative to a product produced using a faster speed. A faster atomizer speed typically creates finer droplets in the atomization cloud. Normally, the finer droplets dry faster than less fine droplets, and the resulting product has a smaller particle size distribution relative to a product produced with slower atomizer speed.
  • the smaller particles can be more difficult to separate, ultimately translating into less product percent yield recovery, such as when a separation cyclone is used.
  • Particles made with a faster atomizer speed will generally have more entrapped and void air both inside the particles and between the particles.
  • a faster atomizer speed can often be used to allow for an increased feed rate and/or air throughput to the dryer while still producing a product with minimal moisture content.
  • Faster atomizer speeds can be particularly useful with feeds having a high viscosity, solids content or Brix value.
  • Slower atomizer speeds can be particularly useful with feed solutions having a low solids content or Brix value.
  • Slower atomizer speeds can often be used to achieve instant properties of the dried product, such as solubility, full dispersibility and wettability.
  • pressure typically can be varied to control the moisture content, bulk density and particle size distribution in the final dried product. In general, increasing pressure results in effects similar to those resulting from increasing atomizer wheel speed.
  • nozzle size typically can be varied to control the moisture content, bulk density and particle size distribution in the final dried product. In general, decreasing nozzle size results in effects similar to those resulting from increasing atomizer wheel speed.
  • the atomizer wheel operates at a rotational speed of from about 10,000 to about 28,000 rpm. In some embodiments, the atomizer wheel operates at a speed of from about 10,000 to about 15,000 rpm. In some embodiments, the atomizer wheel operates at a speed of about 10,000 rpm. In some embodiments, the atomizer wheel operates at a speed of about 12,300 rpm. In some embodiments, the atomizer wheel operates at a speed of about 14,000 rpm.
  • the atomizer wheel operates at a speed of from about 20,000 to about 26,000 rpm. In some embodiments, the atomizer wheel operates at a speed of about 25,500 rpm. In some embodiments, the atomizer has a peripheral speed of from about 52 to about 147 meters/sec. In some embodiments, the atomizer diameter is about 120 mm, the atomizer speed is about 25,500 rpm, and the peripheral speed is about 160 meters/sec.
  • solubility of the FL product is improved by varying one or more process conditions.
  • the spray-drying is conducted in a manner that minimizes the exposure of the desired FL product to elevated temperatures.
  • the retention time inside the dryer is minimized.
  • a high air throughput is used.
  • the FL feed solution is not heated before spray-drying or is heated using a minimal temperature (e.g ., no greater than 60°C) and/or minimal heating time before the spray-drying.
  • a low atomizer speed is used to obtain a larger particle size distribution.
  • a combination of the foregoing is used.
  • the spray dryer is a co-current spray dryer. In some embodiments, the spray dryer is a counter-current spray dryer. In a co-current spray dryer, the air is blown into the drying chamber in the same direction as the liquid. In contrast, in a counter- current spray dryer the air and liquid enter the drying chamber in opposite directions.
  • the air and liquid both enter the drying chamber from the top.
  • the atomized liquid contacts the hot air and evaporates.
  • the dried powder and the moisture- containing air are discharged from the bottom of the drying chamber into a separation cyclone, where the dried powder is separated from the air.
  • the air is vented from the spray dryer into the atmosphere.
  • the dried powder is collected from the separation cyclone.
  • The“air outlet temperature” is the temperature of the air when it exits the spray dryer. In some embodiments, the air outlet temperature is from about 80 to about 1 l0°C. In some embodiments, the air outlet temperature is from about 100 to about 1 l0°C. In some embodiments, the air outlet temperature is about l04°C.
  • a higher solids content or Brix value in the feed solution means that there is less liquid to evaporate during the spray-drying process. This, in turn, generally allows for a lower air outlet temperature to be used, and tends to result in an increased bulk density, particle size distribution, separation efficiency (in, for example, a separation cyclone), and greater overall production rate.
  • the spray dryer is attached to an external fluid bed.
  • the dried powder is collected from the separation cyclone on the fluid bed and undergoes a second round of drying.
  • the fluid bed provides a humid environment that causes small particles to clump together, thereby creating a dried powder with larger particle size. Such powders are less dusty and flow more readily, which makes them easier to handle.
  • water is added by, for example, two fluid nozzles to create the agglomeration.
  • the FL product comprises 2’-FL. In some embodiments, the FL product comprises no 3-FL. In some embodiments, the FL product comprises no fucosyllactose other than 2’-FL.
  • the FL product comprises 3-FL. In some embodiments, the FL product comprises no 2’-FL. In some embodiments, the FL product comprises no fucosyllactose other than 3-FL.
  • the FL product comprises both 2’-FL and 3-FL.
  • This specification also provides an FL in powder form, wherein the FL is 2’-FL or 3-FL, having a loose bulk density of from about 500 to about 700 g/L, a lOOx tapped bulk density of from about 600 to about 850 g/L, a 625x tapped bulk density of from about 600 to about 900 g/L and/or a l250x tapped bulk density of from about 650 to about 1000 g/L.
  • “Bulk density” is the weight of the particles of a particulate solid (such as a powder) in a given volume, and is expressed in grams per litre (g/L). The total volume that the particles of a particulate solid occupy depends on the size of the particles themselves and the volume of the spaces between the particles. Entrapped air between and inside the particles also can affect the bulk density. Thus a particulate solid consisting of large, porous particles with large inter-particulate spaces will have a lower bulk density than a particulate solid consisting of small, non-porous particles that compact closely together. Bulk density can be expressed in two forms:“loose bulk density” and“tapped bulk density”.
  • Loose bulk density is the weight of a particulate solid divided by its volume where the particulate solid has been allowed to settle into that volume of its own accord (e.g. a powder poured into a container).
  • Tapped bulk density is the weight of a particulate solid divided by its volume where the particulate solid has been tapped and allowed to settle into the volume a precise number of times. The number of times the particulate solid has been tapped is typically when stating the tapped bulk density.
  • “lOOx tapped bulk density” refers to the bulk density of the particulate solid after it has been tapped 100 times.
  • Loose bulk density may be measured using a measuring cylinder and weighing scales: the particulate solid is poured into the measuring cylinder and the weight and volume of the particulate solid; weight divided by volume gives the loose bulk density.
  • Tapped bulk density can be measured using the same technique, with the addition of tapping the measuring cylinder a set number of times before measuring weight and volume. Automation of tapping ensures the number, timing and pressure of individual taps is accurate and consistent. Automatic tapping devices are readily available, an example being the Jolting Stampfvolumeter (STAV 203) from J. Englesmann AG.
  • the FL has a loose bulk density of from about 600 to about 700 g/L. In some embodiments, the FL has a loose bulk density of about 693 g/L. In some embodiments, the FL has a loose bulk density of from about 500 to about 600 g/L. In some embodiments, the FL has a loose bulk density of about 582 g/L.
  • the FL has a lOOx tapped bulk density of from about 750 to about 850 g/L. In some embodiments, the FL has a lOOx tapped bulk density of about 814 g/L. In some embodiments, the FL has lOOx tapped bulk density of from about 600 to about 700 g/L. In some embodiments, the FL has a lOOx tapped bulk density of about 699 g/L.
  • the FL has a 625x tapped bulk density of from about 750 to about 900 g/L. In some embodiments, the FL has a 625x tapped bulk density of about 833 g/L. In some embodiments, the FL has a 625x tapped bulk density of from about 700 to about 800 g/L. In some embodiments, the FL has a 625x tapped bulk density of about 771 g/L.
  • the FL has a l250x tapped bulk density of from about 850 to about 900 g/L. In some embodiments, the FL has a l250x tapped bulk density of about 854 g/L. In some embodiments, the FL has a l250x tapped bulk density of from about 750 to about 800 g/L. In some embodiments, the FL has a l250x tapped bulk density of about 782 g/L.
  • the FL has a loose bulk density of from about 600 to about 700 g/L, a lOOx tapped bulk density of from about 750 to about 850 g/L, a 625x tapped bulk density of from about 750 to about 900 g/L and/or a l250x tapped bulk density of from about 850 to about 900 g/L.
  • the FL has a loose bulk density of about 693 g/L, a lOOx tapped bulk density of about 814 g/L, a 625x tapped bulk density of about 833 g/L and/or a l250x tapped bulk density of about 854 g/L.
  • the FL has a loose bulk density of from about 500 to about 600 g/L, a lOOx tapped bulk density of from about 600 to about 700 g/L, a 625x tapped bulk density of from about 700 to about 800 g/L and/or a l250x tapped bulk density of from about 750 to about 800 g/L. In some embodiments, the FL has a loose bulk density of about 582 g/L, a lOOx tapped bulk density of about 699 g/L, a 625x tapped bulk density of about 771 g/L and/or a l250x tapped bulk density of about 782 g/L.
  • the FL has a moisture content of less than 9% (by weight) water. In some embodiments, the FL has a moisture content of no greater than 5% (by weight) water. In some embodiments, the spray dryer is operated to achieve a moisture content of from about 3.0 to 5.0% (by weight). In some embodiments, the FL has a moisture content of less than 5% (by weight) water. In some embodiments, the FL has a moisture content of less than about 2.3% (by weight) water. In some such embodiments, the FL has a moisture content of from about 1.80 to about 2.25% (by weight) water. In some embodiments, the FL has a moisture content of from about 2.12 to about 2.21% (by weight) water. In some embodiments, the FL has a moisture content of from about 2.0 about 2.1% (by weight) water.
  • the FL solution comprises 2’-FL, has a Brix value of 47.48 %Brix and is at a temperature of about 30°C before spray drying, the spray drying uses air with an inlet temperature of l35°C and an outlet temperature of l04°C, and the spray dryer is a co-current spray dryer comprising an atomizer wheel that operates at 25, 136 rpm.
  • the FL prepared is 2’-FL in powder form, has a loose bulk density of 601 g/L, a lOOx tapped bulk density of 772 g/L, a 625x tapped bulk density of 832 g/L and a moisture content of 2.12-2.21% (by weight) water.
  • the FL solution comprises 2’-FL, has a Brix value of 50.3 %Brix and is at a temperature of less than 35°C before spray drying, the spray drying uses air with an inlet temperature of l80°C and an outlet temperature of l02°C, and the spray dryer is a co-current spray dryer comprising an atomizer wheel that operates at 12,300 rpm.
  • the FL prepared is 2’-FL in powder form, has a loose bulk density of 693 g/L, a lOOx tapped bulk density of 814 g/L, a 625x tapped bulk density of 833 g/L and a l250x tapped bulk density of 854 g/L.
  • the FL solution comprises 3-FL, has a Brix value of 53.9 %Brix and is at a temperature of less than 5 °C before spray drying, the spray drying uses air with an inlet temperature of l80°C and an outlet temperature of l04°C, and the spray dryer is a co-current spray dryer comprising an atomizer wheel that operates at 25,500 rpm.
  • the FL prepared is 3-FL in powder form, has a loose bulk density of 507 g/L, a lOOx tapped bulk density of 625 g/L, a 625x tapped bulk density of 686 g/L, a l250x tapped bulk density of 707 g/L and a moisture content of 2.0-2.1% (by weight) water.
  • the FL solution comprises 3-FL, has a Brix value of 51.9 %Brix and is at a temperature of about 20°C before spray drying, the spray drying uses air with an inlet temperature of l80°C and an outlet temperature of l03°C, and the spray dryer is a co current spray dryer comprising an atomizer wheel that operates at 25,500 rpm.
  • the FL prepared is 3-FL in powder form, has a loose bulk density of 582 g/L, a lOOx tapped bulk density of 699 g/L, a 625x tapped bulk density of 771 g/L and a l250x tapped bulk density of 782 g/L.
  • the FL is prepared by the process disclosed in this specification.
  • This specification additionally provides an FL as disclosed in this specification for use in prevention and/or treatment of a disease.
  • This specification provides a prebiotic product comprising the FL disclosed in this specification.
  • A“prebiotic” is a substance that promotes growth of microorganisms beneficial to the host, and, in particular, those in the gastrointestinal tract.
  • a prebiotic product comprises multiple prebiotics, including the FL disclosed in this specification.
  • This specification also provides a process for preparing a prebiotic product, comprising conducting the process disclosed in this specification; obtaining the dried FL; and admixing the dried FL with one or more prebiotic product ingredients.
  • Suitable prebiotic product ingredients are known in the art.
  • the prebiotic product comprises other prebiotic molecules, such as other HMOs and various plant polysaccharides such as inulin, pectin, b-glucan and xylooligosaccharide.
  • the prebiotic product ingredients comprises other sugars, such as lactose, glucose and galactose; thickeners, such as gum arabic; and acidity regulators, such as trisodium citrate.
  • A“probiotic” product is typically a dietary supplement containing live microorganisms that replace or add to gastrointestinal microflora, to the benefit of the recipient.
  • This specification provides a process for preparing a probiotic product, comprising conducting the process disclosed in this specification; obtaining the dried FL; and admixing the dried FL with one or more probiotic product ingredients.
  • Suitable probiotic product ingredients are known in the art.
  • At least one probiotic product ingredient is a live microorganism (which is the“probiotic” itself).
  • multiple probiotic product ingredients are different live microorganisms. Examples of such microorganisms include Lactobacillus species such as L. acidophilus and L. bulgaricus , Bifidobacterium species such as B. animalis and B. longum , and Saccharomyces boulardii.
  • Other probiotic ingredients include water, skimmed milk, substrates for microorganism growth such as sucrose, dextrose and/or other HMOs, and flavourings.
  • This specification also provides a food comprising the FL disclosed in this specification.
  • the food is an infant formula.
  • Infant formula is a manufactured food for feeding to infants as a complete or partial substitute for human breast milk.
  • infant formula is sold as a powder and prepared for bottle- or cup- feeding to an infant by mixing with water.
  • the molecular, and therefore nutritional, composition of infant formula is typically designed to be roughly the same as human breast milk.
  • the FL disclosed in this specification is included in infant formula to provide nutritional benefits similar to those provided by HMOs in human breast milk.
  • This specification further provides a process for preparing a food, comprising conducting the process disclosed in this specification; obtaining the dried FL; and admixing the dried FL with one or more food ingredients.
  • the food is an infant formula.
  • Suitable food ingredients for admixing with the dried FL include infant formula ingredients.
  • Infant formula ingredients are known in the art and include lactose, vegetable oils such as palm, rapeseed, coconut and/or sunflower oil, fish oil, emulsifier such as soya lecithin, whey, casein, other HMOs, vitamins such as vitamins A, B 6 , B12, C and D, and minerals such as potassium citrate, calcium citrate, magnesium chloride, sodium chloride, sodium citrate and calcium phosphate.
  • Example 1 The process described in Example 1 was carried out a further five times. For each of these examples, the characteristics of the 2-FL solution and the dried 2’-FL product, as well as the spray dryer settings, are presented in Table 4.
  • the drying process lasted for 532 minutes.
  • Example 7 The process described in Example 7 was carried out a further three times. For each of these examples, the characteristics of the 3-FL solution and the dried 3-FL product, as well as the spray dryer settings, are presented in the Table 8. Table 8

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Biochemistry (AREA)
  • Molecular Biology (AREA)
  • Food Science & Technology (AREA)
  • General Health & Medical Sciences (AREA)
  • Nutrition Science (AREA)
  • Biotechnology (AREA)
  • Polymers & Plastics (AREA)
  • Genetics & Genomics (AREA)
  • Mycology (AREA)
  • Pediatric Medicine (AREA)
  • Emergency Medicine (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

La présente invention concerne un procédé de préparation d'un fucosyllactose (FL) séché à partir d'une solution de FL par séchage par pulvérisation. La présente invention concerne en outre un FL sous forme de poudre ayant une densité apparente élevée, telle qu'obtenue par le procédé décrit dans la présente spécification, ainsi que des prébiotiques, des probiotiques et des aliments comprenant le FL.
PCT/US2019/017811 2018-02-19 2019-02-13 Procédé de séchage par pulvérisation de solutions de fucosyllactose et compositions de produit associées WO2019160922A1 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
KR1020207026496A KR20210013007A (ko) 2018-02-19 2019-02-13 푸코실락토스 용액을 분무 건조하는 방법 및 관련 제품 조성물
JP2020566197A JP2021514388A (ja) 2018-02-19 2019-02-13 噴霧乾燥フコシルラクトース溶液のプロセスおよび関連産物の組成物
CN201980026156.8A CN112020568A (zh) 2018-02-19 2019-02-13 用于喷雾干燥岩藻糖基乳糖溶液的方法及相关产品组合物
AU2019222670A AU2019222670A1 (en) 2018-02-19 2019-02-13 Process for spray drying fucosyllactose solutions and related product compositions
CA3091514A CA3091514A1 (fr) 2018-02-19 2019-02-13 Procede de sechage par pulverisation de solutions de fucosyllactose et compositions de produit associees
US16/970,800 US20210059282A1 (en) 2018-02-19 2019-02-13 Process for Spray Drying Fucosyllactose Solutions and Related Product Compositions
EP19754060.2A EP3755819A4 (fr) 2018-02-19 2019-02-13 Procédé de séchage par pulvérisation de solutions de fucosyllactose et compositions de produit associées

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
US201862632153P 2018-02-19 2018-02-19
US62/632,153 2018-02-19
US201862648428P 2018-03-27 2018-03-27
EP18164250.5 2018-03-27
EP18164250.5A EP3546060A1 (fr) 2018-03-27 2018-03-27 Procédé de séchage par pulvérisation de solutions de fucosyllactose et de compositions de produit correspondantes
US62/648,428 2018-03-27

Publications (1)

Publication Number Publication Date
WO2019160922A1 true WO2019160922A1 (fr) 2019-08-22

Family

ID=67619652

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2019/017811 WO2019160922A1 (fr) 2018-02-19 2019-02-13 Procédé de séchage par pulvérisation de solutions de fucosyllactose et compositions de produit associées

Country Status (1)

Country Link
WO (1) WO2019160922A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3822282A1 (fr) 2019-11-18 2021-05-19 DuPont Nutrition Biosciences ApS Procédé d'élimination d'un agent antimousse dans une solution comprenant un oligosaccharide du lait humain et compositions associées
WO2022072333A1 (fr) 2020-09-29 2022-04-07 Dupont Nutrition Biosciences Aps Procédé de purification d'un oligosaccharide de lait humain et compositions associées
WO2022072323A1 (fr) 2020-09-29 2022-04-07 Dupont Nutrition Biosciences Aps Procédé de purification d'un oligosaccharide de lait maternel et compositions associées
WO2022096613A1 (fr) * 2020-11-09 2022-05-12 Basf Se Obtention de solutions de hmo hautement concentrées par osmose inverse
WO2022223652A1 (fr) * 2021-04-22 2022-10-27 Dsm Ip Assets B.V. Procédé de séchage pour hmos
WO2023066907A1 (fr) 2021-10-18 2023-04-27 Dsm Ip Assets B.V. Procédé de préparation d'un produit hmo amorphe par séchage
WO2024003222A1 (fr) 2022-06-29 2024-01-04 Inbiose N.V. Saccharide fucosylé destiné à être utilisé dans la prévention ou le traitement d'une maladie bactérienne

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6146670A (en) * 1997-03-31 2000-11-14 Abbott Laboratories Nutritional formulations containing oligosaccharides
US20160237104A1 (en) * 2013-10-04 2016-08-18 Jennewein Biotechnologie Gmbh Process for purification of neutral human milk oligosaccharide using simulated moving bed chromatography
US20170202864A1 (en) * 2014-07-21 2017-07-20 Abbott Laboratories Nutrient delivery system with human milk oligosaccharides

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6146670A (en) * 1997-03-31 2000-11-14 Abbott Laboratories Nutritional formulations containing oligosaccharides
US20160237104A1 (en) * 2013-10-04 2016-08-18 Jennewein Biotechnologie Gmbh Process for purification of neutral human milk oligosaccharide using simulated moving bed chromatography
US20170202864A1 (en) * 2014-07-21 2017-07-20 Abbott Laboratories Nutrient delivery system with human milk oligosaccharides

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
"Stage 6 Harmonization: Official August 1, 2015: 〈616〉 Bulk Density and Tapped Density of Powders", THE UNITED STATES PHARMACOPEIAL CONVENTION, 1 August 2015 (2015-08-01), pages 1 - 3, XP009522700, Retrieved from the Internet <URL:https://www.usp.org/sites/default/files/usp/document/harmonization/gen-chapter/bulk_density.pdf> [retrieved on 20190403] *
See also references of EP3755819A4 *

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3822282A1 (fr) 2019-11-18 2021-05-19 DuPont Nutrition Biosciences ApS Procédé d'élimination d'un agent antimousse dans une solution comprenant un oligosaccharide du lait humain et compositions associées
WO2022072333A1 (fr) 2020-09-29 2022-04-07 Dupont Nutrition Biosciences Aps Procédé de purification d'un oligosaccharide de lait humain et compositions associées
WO2022072323A1 (fr) 2020-09-29 2022-04-07 Dupont Nutrition Biosciences Aps Procédé de purification d'un oligosaccharide de lait maternel et compositions associées
WO2022096613A1 (fr) * 2020-11-09 2022-05-12 Basf Se Obtention de solutions de hmo hautement concentrées par osmose inverse
WO2022223652A1 (fr) * 2021-04-22 2022-10-27 Dsm Ip Assets B.V. Procédé de séchage pour hmos
WO2023066907A1 (fr) 2021-10-18 2023-04-27 Dsm Ip Assets B.V. Procédé de préparation d'un produit hmo amorphe par séchage
WO2024003222A1 (fr) 2022-06-29 2024-01-04 Inbiose N.V. Saccharide fucosylé destiné à être utilisé dans la prévention ou le traitement d'une maladie bactérienne

Similar Documents

Publication Publication Date Title
WO2019160922A1 (fr) Procédé de séchage par pulvérisation de solutions de fucosyllactose et compositions de produit associées
US20210059282A1 (en) Process for Spray Drying Fucosyllactose Solutions and Related Product Compositions
Bustamante et al. Effective Lactobacillus plantarum and Bifidobacterium infantis encapsulation with chia seed (Salvia hispanica L.) and flaxseed (Linum usitatissimum L.) mucilage and soluble protein by spray drying
CN111670257A (zh) 无定形糖组合物
Sarabandi et al. Physical properties of spray dried grape syrup as affected by drying temperature and drying aids
US3194682A (en) Sugar product and method of producing same
Dubkova et al. Using Jerusalem artichoke powder in functional food production.
Farías‐Cervantes et al. Effect of spray drying of agave fructans, nopal mucilage and aloe vera juice
Kothakota et al. Characteristics of spray dried dahi powder with maltodextrin as an adjunct
Padma Ishwarya et al. Spray drying
CN110122778A (zh) 一种米粉制造方法
KR20220155595A (ko) 고체 hmo 생성물을 제공하는 방법, 및 이에 의해 수득된 고체 hmo 생성물
CN106107056A (zh) 一种含纽甜微囊型甜味剂的制备方法
JP6727576B1 (ja) 麦類若葉乾燥粉末造粒物の飲食品組成物及びその製造方法
Schuck Understanding the factors affecting spray-dried dairy powder properties and behavior
Chávez-Rodríguez et al. Optimization of Agave tequilana Weber var. Azul juice spray drying process
Bringas-Lantigua et al. Influence of process conditions on the physicochemical properties of honey powder produced by spray drying
Habtegebriel et al. Surface fat and insolubility of whole camel milk powders as affected by spray drying operating parameters
Osman et al. Spray drying of roselle-pineapple juice effects of inlet temperature and maltodextrin on the physical properties
Farimin et al. Physical properties of powdered Roselle-pineapple juice-effects of maltodextrin
KR102648906B1 (ko) 식이섬유 함유 감미 조성물 및 이의 제조 방법
Zare et al. Determination of physical properties of sour orange juice powder produced by a spray dryer
Joshi et al. Spray Drying: Principles and Applications
Aldrete-Herrera et al. Study of the rheological and physicochemical properties of fructan fractions of Agave tequilana cv. Cenizo
Bartkowiak et al. Novel polymer systems and additives to protect bioactive substances applied in spray‐drying

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 19754060

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 3091514

Country of ref document: CA

ENP Entry into the national phase

Ref document number: 2020566197

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2019222670

Country of ref document: AU

Date of ref document: 20190213

Kind code of ref document: A

ENP Entry into the national phase

Ref document number: 2019754060

Country of ref document: EP

Effective date: 20200921