Classifications

• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K47/00—Medicinal preparations characterised by the non-active ingredients used, e.g. carriers or inert additives; Targeting or modifying agents chemically bound to the active ingredient
  • A61K47/44—Oils, fats or waxes according to two or more groups of A61K47/02-A61K47/42; Natural or modified natural oils, fats or waxes, e.g. castor oil, polyethoxylated castor oil, montan wax, lignite, shellac, rosin, beeswax or lanolin
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K9/00—Medicinal preparations characterised by special physical form
  • A61K9/10—Dispersions; Emulsions
  • A61K9/107—Emulsions ; Emulsion preconcentrates; Micelles
  • A61K9/1075—Microemulsions or submicron emulsions; Preconcentrates or solids thereof; Micelles, e.g. made of phospholipids or block copolymers
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K47/00—Medicinal preparations characterised by the non-active ingredients used, e.g. carriers or inert additives; Targeting or modifying agents chemically bound to the active ingredient
  • A61K47/06—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite
  • A61K47/08—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite containing oxygen, e.g. ethers, acetals, ketones, quinones, aldehydes, peroxides
  • A61K47/10—Alcohols; Phenols; Salts thereof, e.g. glycerol; Polyethylene glycols [PEG]; Poloxamers; PEG/POE alkyl ethers
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K47/00—Medicinal preparations characterised by the non-active ingredients used, e.g. carriers or inert additives; Targeting or modifying agents chemically bound to the active ingredient
  • A61K47/06—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite
  • A61K47/08—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite containing oxygen, e.g. ethers, acetals, ketones, quinones, aldehydes, peroxides
  • A61K47/12—Carboxylic acids; Salts or anhydrides thereof
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K47/00—Medicinal preparations characterised by the non-active ingredients used, e.g. carriers or inert additives; Targeting or modifying agents chemically bound to the active ingredient
  • A61K47/06—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite
  • A61K47/08—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite containing oxygen, e.g. ethers, acetals, ketones, quinones, aldehydes, peroxides
  • A61K47/14—Esters of carboxylic acids, e.g. fatty acid monoglycerides, medium-chain triglycerides, parabens or PEG fatty acid esters
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K47/00—Medicinal preparations characterised by the non-active ingredients used, e.g. carriers or inert additives; Targeting or modifying agents chemically bound to the active ingredient
  • A61K47/06—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite
  • A61K47/22—Heterocyclic compounds, e.g. ascorbic acid, tocopherol or pyrrolidones
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K47/00—Medicinal preparations characterised by the non-active ingredients used, e.g. carriers or inert additives; Targeting or modifying agents chemically bound to the active ingredient
  • A61K47/06—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite
  • A61K47/24—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite containing atoms other than carbon, hydrogen, oxygen, halogen, nitrogen or sulfur, e.g. cyclomethicone or phospholipids
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K9/00—Medicinal preparations characterised by special physical form
  • A61K9/0012—Galenical forms characterised by the site of application
  • A61K9/0019—Injectable compositions; Intramuscular, intravenous, arterial, subcutaneous administration; Compositions to be administered through the skin in an invasive manner
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K9/00—Medicinal preparations characterised by special physical form
  • A61K9/10—Dispersions; Emulsions
  • A61K9/107—Emulsions ; Emulsion preconcentrates; Micelles
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
  • B01F23/40—Mixing liquids with liquids; Emulsifying
  • B01F23/41—Emulsifying
  • B01F23/4105—Methods of emulsifying
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
  • B01F23/40—Mixing liquids with liquids; Emulsifying
  • B01F23/41—Emulsifying
  • B01F23/413—Homogenising a raw emulsion or making monodisperse or fine emulsions
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
  • B01F23/40—Mixing liquids with liquids; Emulsifying
  • B01F23/45—Mixing liquids with liquids; Emulsifying using flow mixing
  • B01F23/452—Mixing liquids with liquids; Emulsifying using flow mixing by uniting flows taken from different parts of a receptacle or silo; Sandglass-type mixing
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
  • B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
  • B01F25/23—Mixing by intersecting jets
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
  • B01F27/27—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
  • B01F33/80—Mixing plants; Combinations of mixers
  • B01F33/82—Combinations of dissimilar mixers
  • B01F33/821—Combinations of dissimilar mixers with consecutive receptacles
  • B01F33/8212—Combinations of dissimilar mixers with consecutive receptacles with moving and non-moving stirring devices
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
  • B01F23/40—Mixing liquids with liquids; Emulsifying
  • B01F23/41—Emulsifying
  • B01F23/414—Emulsifying characterised by the internal structure of the emulsion
  • B01F23/4145—Emulsions of oils, e.g. fuel, and water

Definitions

• O / W emulsion Process for producing an O / W emulsion.
• the invention relates to a process for producing an O / W emulsion, an O / W emulsion and a plant for producing an O / W emulsion.
• An emulsion is a finely divided mixture of two normally immiscible liquids without visible segregation.
• One liquid (phase) forms small drops distributed in the other liquid.
• the phase that forms drops is called the inner or the disperse phase.
• the phase in which the drops float is called outer or continuous phase.
• Emulsions of water and oil are distinguished in water-in-oil emulsion (W / O emulsion) and oil-in-water emulsion (O / W emulsion).
• emulsifier Another important component of emulsions is the emulsifier, which facilitates the formation of droplets and counteracts segregation (phase separation).
• the components used to prepare an emulsion are first premixed into a coarsely dispersed preemulsion, which may also be referred to as a raw or pre-emulsion or premix. Subsequently, a homogenization, wherein a drop comminution of the disperse phase takes place (fine emulsification). The droplet size spectrum of the crude or pre-emulsion shifts significantly towards smaller droplets.
• O / W emulsions for parenteral use are usually prepared by first premixing an oil phase and water phase by means of a rotor-stator agitator to a pre-emulsion and then homogenizing by means of a piston-gap homogenizer.
• Piston-gap homogenizers are so-called high-pressure homogenizers which are based on a high-pressure pump and a homogenizing nozzle. The high pressure pump builds up energy, which can then be used by relaxing in a Homogenisierventil for drop crushing. In a piston-gap homogenizer pressures of 100 to several hundred bar can be realized.
• the pre-emulsion In a piston-gap homogenizer, the pre-emulsion is usually pumped through a centric inlet bore, the pre-emulsion then passing through a radial gap between a valve seat and a valve stem.
• shear and expansion forces, impingement flows and, to a significant extent, cavitation forces are generally effective.
• Cavitation is the formation and dissolution of cavities in liquids due to pressure fluctuations. The cavitation is caused for example by very fast moving objects in the liquid (for example, by propeller or stirrer) or by rapid movement of liq fluid such as through a nozzle and by the action of ultrasound.
• O / W emulsions intended for parenteral administration must meet certain specifications.
• such emulsions for compliance with minimum medical standards should not exceed a mean drop diameter of 500 nm, preferably 350 nm.
• O / W emulsions should have a so-called pFAT5 value of ⁇ 0.05%. This value defines the percentage of drops within an oil phase of an O / W emulsion with a diameter, in particular average diameter, of 5 pm to 50 pm. This is a safety parameter for avoiding fat embolism in patients.
• a disadvantage of conventional processes for the production of O / W emulsions are long process times and in particular often only limited or insufficient process control options, in particular with regard to the quality of the O / W emulsions to be produced. For example, slight deviations from process parameters can lead to incorrect batches and consequently to batch destruction to a considerable extent.
• the invention relates to a process for the preparation of an oil-in-water emulsion, hereinafter abbreviated as O / W emulsion, in particular for parenteral administration.
• the process comprises the following steps: a) providing an oil phase and a water phase, b) premixing, i. Pre-homogenizing or pre-emulsifying the oil phase and the water phase to an oil-in-water pre-emulsion, i.
• O / W preemulsion an oil-in-water preemulsion, hereinafter abbreviated as O / W preemulsion (O / W preemulsion); and c) homogenizing the O / W preemulsion to an O / W emulsion by means of at least one counter jet dispersant.
• water phase is understood to mean water or a water-containing liquid, in particular an aqueous solution, which in the finished O / W emulsion, i. in the O / W emulsion produced by the process according to the invention, which forms an outer or continuous phase.
• oil phase is to be understood as meaning an oil and / or lipid and / or an oil and / or lipid-containing liquid, in particular an oil and / or lipid-containing solution, which or in the form of Drops in the finished O / W emulsion, ie in the O / W emulsion produced by the process of the invention, forming the inner or disperse phase.
• the term "drops" is understood to mean oil drops and / or lipid drops, ie drops consisting of at least one oil and / or at least one lipid, and / or drops containing oil and / or lipids, which are the internal or disperse Phase of the O / W preemulsion and / or O / W emulsion.
• the O / W preemulsion is distinguished by a broader droplet diameter distribution and / or by larger diameter drops, in particular larger average diameters, than the O / W emulsion.
• counter jet disperser is to be understood as meaning a high pressure homogenizer in which two or more jets of a preemulsion (primary or crude emulsion) meet at least two, preferably two opposite, bores or channels in a drop comminution zone. Due to the meeting of the pre-emulsion jets, droplet comminution of drops contained in the preemulsion takes place, in particular under the action of shear forces.
• the aforementioned drop comminution zone can therefore also be referred to as a shear zone.
• the extent of drop comminution is particularly dependent on the conveying speed at which the O / W preemulsion or O / W preemulsion jets are conveyed within the counter jet disperser.
• the conveying speed of the O / W preemulsion or O / W preemulsion jets is controllable via a pressure which is generated by a pump, in particular a high-pressure pump, of the counter-jet disperser.
• At least one counter jet dispersant can, as will be explained in more detail below, a Schmidtdispergator or, which is preferred, a plurality of Schwarzstrahldispergatoren, i. several Schwarzstrahldispergatoren mean.
• the at least one counter jet disperser provided for carrying out step c) preferably has at least two, in particular two, preferably two opposite, channels or more channels.
• the channels have, for example, an inner diameter in the micrometer range.
• the channels of the at least one counter jet disperser can furthermore have in particular a Y-shaped configuration or arrangement.
• Preemulsification of an oil phase and water phase and subsequent high-pressure homogenization using at least one counter jet disperser on the one hand a significant reduction in production times for O / W emulsions and on the other hand better controllability of the quality of the O / W emulsions to be produced and in particular the production of high quality O / W emulsions achievable.
• a shortening of the process times by up to 75% is possible by means of the method according to the invention.
• production costs can be saved to a considerable extent and the number of producible emulsion batches per unit of time can be significantly increased. Overall, this leads to a significant increase in productivity.
• counter jet dispersants are typically static, i. have constant, chamber dimensions. This facilitates the implementation of scale-up processes, for example, when using multiple counter jet dispersers, the number of chambers can be upscaled linearly with the volume.
• the inventive method allows in particular the production of O / W emulsions having a droplet diameter, in particular mean droplet diameter (determined according to
• Photon correlation spectroscopy from 180 nm to 340 nm, in particular 200 nm to 320 nm, preferably 200 nm to 300 nm, particularly preferably 240 nm to 280 nm.
• the pFAT5 value of the O / W emulsions to be produced can be better controlled and in particular significantly reduced.
• the risk of fatty embolism in the case of parenteral administration of a O / W emulsion produced by the O / W emulsion according to the invention can be significantly reduced.
• the water phase provided according to the invention can be provided by using an emulsifier, ie by adding an emulsifier to water or a water-containing liquid.
• the water phase may be provided by dissolving an emulsifier in water or a liquid containing water.
• the water phase to a temperature of 40 ° C to 80 ° C, in particular 50 ° C to 70 ° C, heated.
• An emulsifier which can be used is a compound which is selected from the group consisting of phospholipids, phospholipids of animal origin, phospholipids of plant origin, lecithins such as egg lecithin, krill phospholipids and mixtures of at least two of the emulsifiers mentioned.
• the water phase can be provided using an additive, ie, by adding an additive to water or a water-containing liquid.
• the water phase can be provided by dissolving an additive in water or a liquid containing water.
• a compound can be used, which is selected from the group consisting of emulsifying aid, stabilizer, Isotonmaschineszusatz and mixture of at least two of said additives.
• the emulsifying aid for example, an alkali salt of a long-chain fatty acid, for example, a fatty acid having 16 to 18 carbon atoms can be used.
• a stabilizer or isotonization additive for example, a polyhydric alcohol, in particular selected from the group consisting of glycerol, glucose, xylitol and mixtures of at least two of said stabilizers or isotonization additives, are used.
• the oily phase may be provided using an oil and / or lipid which is preferably selected from the group consisting of oils of vegetable origin, medium chain triglycerides (MCT), oils of animal origin, oils of marine origin and mixtures of at least two of said oils or lipids.
• oils of vegetable origin for example, safflower oil and / or soybean oil can be used. These oils are characterized by a high proportion of polyunsaturated fatty acids from the w-6 series (predominantly linoleic acid, 18: 2 co-6), while their content of w-3 fatty acids (practically exclusively as a-linolenic acid, 18: 3 co-3) is low.
• Mid-chain triglycerides have a carbon chain length of 6 to 14 carbon atoms, more preferably 8 to 10 carbon atoms.
• oils of marine origin for example, fish oils and / or krill oils can be used.
• the fish oils derived from cold-water fish are, like Krill oils obtained from krill, characterized by a high proportion of polyunsaturated fatty acids (mainly eicosapentaenoic acid, EPA, 20: 5 co-3 and docosahexaenoic acid, DHA, 20: 6 ⁇ o-3) while their content of w-6 fatty acids is low.
• Suitable fish oils are, for example, those which are obtained industrially to a significant extent from cold-water fish.
• Fish oils generally contain triglycerides of fatty acids having 12 to 22 carbon atoms.
• oils may be used which are selected from the group consisting of sardine oil, salmon oil, herring oil, mackerel oil and mixtures of at least two of the said fish oils.
• corresponding fish oil concentrates and / or krill oils can be used.
• the oil phase can be prepared using an emulsifier, ie by adding an emulsifier to an oil or oil mixture, an oily liquid, a lipid or Lipid mixture or a lipid-containing liquid, in particular by dissolving an emulsifier in an oil or oil mixture, an oily liquid, a lipid or lipid mixture or a lipid-containing liquid, are provided.
• the emulsifier used in this case may be a compound which is preferably selected from the group consisting of phospholipids and mixtures of at least two phospholipids.
• the oil phase may be prepared using an additive, i. H. by adding an additive to an oil or oil mixture, an oily liquid, a lipid or lipid mixture or a lipid-containing liquid, in particular by dissolving an additive in an oil or oil mixture, an oily liquid, a lipid or lipid mixture or a lipid-containing liquid.
• an additive for example, an antioxidant, such as a tocopherol and / or physiologically acceptable tocopherol esters, such as a-tocopherol acetate, can be used.
• an emulsifier-containing water phase and an emulsifier-free oil phase can be provided.
• This variant referred to as the English method, for producing an O / W emulsion has the advantage over the continental method described below that often lower amounts of emulsifier are required.
• an emulsifier-free water phase and an emulsifier-containing oil phase can be provided.
• This variant referred to as a continental method, for producing an O / W emulsion has the advantage that it leads to a shortening of the process time owing to the better dispersibility of the phospholipids.
• the inventive method can be operated with particular advantage, in particular without modification of the process sequence and / or without modification of a process plant, both based on the English method and based on the continental method.
• the oil phase and the water phase can already be brought together before carrying out step b).
• the oil phase can be added to the water phase before carrying out step b).
• step b) is carried out by means of at least one rotor-stator-disperser, in particular rotor-stator-stirrer.
• rotor-stator-disperser is understood to mean a dispersant, in particular a stirrer or prehomogenizer, which operates on the rotor-stator principle, ie. a rotor and a stator (so-called rotor-stator system) has.
• About the configuration of the rotor and / or the stator of the at least one rotor-stator disperser can be with particular advantage of the specific energy input for a drop crushing, in particular drop shear, influence.
• the oil phase and the water phase are spatially separated from each other supplied to the at least one rotor-stator-disperser.
• the oil phase and the water phase by means of a coaxial tube, d. H. a tube-in-tube arrangement, or by means of a coaxial tube, d. H. a hose-in-hose assembly to which at least one rotor-stator disperser supplied.
• a coaxial tube d. H. a tube-in-tube arrangement
• a coaxial tube d. H. a hose-in-hose assembly
• the water phase through the middle tube or the middle tube and the oil phase through the middle tube surrounding the (coaxial) outer tube or through the middle tube surrounding (coaxial) outer tube becomes.
• mixed forms of the method can be moved after the configuration of the English method.
• At least one rotor-stator-disperser can, for the purposes of the present invention, a rotor-stator-disperser or a plurality of rotor-stator-dispersants, ie several rotor-stator dispersants, such as two, three, four or five rotor-stator dispersants mean.
• step b) can basically be carried out by means of only one rotor-stator disperser.
• the step b) can be carried out by means of a plurality of rotor-stator dispersants, in particular by means of a plurality of parallel-connected rotor-stator dispersants and / or by means of a plurality of series-connected rotor-stator dispersants.
• step b) can only be carried out by means of parallel-connected rotor-stator dispersants.
• step b) can only be carried out by means of series-connected rotor-stator dispersants.
• Step b) can be performed by commercially available under the designation ULTRA-TURRAX ® line rotor-stator dispersers for example by means of one or a plurality.
• the oil phase and the water phase are passed through a droplet comminution zone, in particular a shear zone, of the at least one rotor-stator disperser.
• drop crusher zone is meant in this context a zone, i. a region or section of the at least one rotor-stator-disperser are understood, within which takes place due to the action of the rotor and / stator, a drop crushing, in particular under the influence of shear forces.
• the process procedure described in this paragraph may also be referred to as forced passage of the oil phase and the water phase through the drop comminution zone, in particular shear zone, of the at least one rotor-stator disperser.
• the O / W preemulsion can be homogenized directly, ie without further intermediate steps, to form an O / W emulsion.
• another is advantageously Shortening the production time and thus achieving a further increase in process productivity.
• the O / W preemulsion may be passed through a buffer or container prior to performing step c).
• the buffer or container is used with particular advantage to maintain the process flow and thus facilitates the coordination between the at least one rotor-stator-disperser and the at least one Jacobstrahldispergator.
• step c) is carried out by means of a pump pressure of 500 bar to 2000 bar, in particular 800 bar to 1900 bar, preferably 1000 bar to 1500 bar.
• the pump pressure disclosed in this paragraph has been found to be particularly advantageous for drop crushing, in particular drop shear, and preferably for realizing a narrow or narrow droplet diameter distribution.
• the term "pump pressure” is to be understood as meaning a pressure generated by a pump, in particular a high-pressure pump, of the at least one counter-jet disperser. This is u.a. responsible for the conveying speed of the O / W preemulsion, in particular of O / W preemulsion jets, within the at least one counter jet disperser. Therefore, the impact pressure of O / W preemulsion jets within a droplet comminution zone, in particular shear zone, of the at least one counter jet disperser and thus the drop comminution and thus the homogenization of the O / W preemulsion to an O / W emulsion can be controlled via the pump pressure.
• the pump pressure in the context of the present invention may also be referred to as homogenization pressure.
• the at least one counter jet disperser at a temperature of the O / W preemulsion of 30 ° C to 80 ° C, in particular 40 ° C to 77.5 ° C, preferably 40 ° C to 75 ° C, particularly preferably 40 ° C to 65 ° C, is operated, or, in other words, the O / W preemulsions when performing section c) a temperature of 30 ° C to 80 ° C, in particular 40 ° C to 77.5 ° C, preferably 40 ° C to 75 ° C, more preferably 40 ° C to 65 ° C, having.
• the temperature disclosed in this paragraph can therefore also be referred to as homogenizing temperature in the sense of the present invention.
• the ones in this attachment revealed temperature has (also) been found to be particularly advantageous for drop crushing, especially drop shear, and preferably for the realization of a narrow or narrow droplet diameter distribution.
• the at least one counter jet disperser may be operated to perform step c) at a pump pressure of 1900 bar and at a temperature of the O / W preemulsion of 40 ° C.
• the at least one counter jet disperser for carrying out step c) can be operated, for example, at a pump pressure of 1500 bar and at a temperature of the O / W preemulsion of 50 ° C.
• the at least one counter jet disperser for carrying out step c) can be operated, for example, at a pump pressure of 1000 bar and at a temperature of the O / W preemulsion of 60 ° C.
• the O / W preemulsion when performing step c) is passed through the at least one counter jet disperser several times, in particular twice, three times, four times or five times.
• step c) by means of a plurality of Jacobstrahldispergatoren, in particular by means of two, three, four or five Jacobstrahldispergatoren performed.
• step c) is carried out by means of a plurality of parallel jet counter-jet dispersers and / or by means of a plurality of counter-jet jet dispersers connected in series.
• a significant improvement in the process quality in particular with respect to the mean droplet diameter and / or the pFAT5 value, can also be achieved.
• this procedural measure (s) can increase process productivity.
• step c) can only be carried out by means of parallel jet counter-jet dispersers.
• step c) can only be carried out by means of counter-jet dispersers connected in series.
• step c) is carried out at least by means of two counter-jet dispersers connected in series, in particular only by means of two counter-jet dispersers connected in series.
• the first counter jet disperser is operated at a higher pump pressure than the second, i. downstream, Gegenstrahldispergator.
• the first i. downstream, Gegenstrahldispergator with a pump pressure of at most 1900 bar, preferably at most 1500 bar, in particular at a pump pressure of 800 bar to 1400 bar, preferably 1000 bar to 1200 bar
• the present invention is further based on the surprising finding that drops with a diameter, in particular average diameter, of 1 pm to 50 pm at a pump pressure of ⁇ 1000 bar, in particular from 500 bar to 800 bar, preferably from 500 bar, preferably crush to let.
• a diameter, in particular average diameter of 1 pm to 50 pm at a pump pressure of ⁇ 1000 bar, in particular from 500 bar to 800 bar, preferably from 500 bar, preferably crush to let.
• the present invention is based on the surprising finding that the first counter jet disperser is operated at a higher pump pressure than the second (downstream) counter jet disperser by means of a pressure cascade, in particular by means of at least two counter jet mixers connected in series, as described in the penultimate paragraph , Produce drops with a diameter, in particular average diameter, ⁇ 500 nm, in particular ⁇ 400 nm, preferably ⁇ 350 nm, in particular from 200 nm to 320 nm, preferably 200 nm to 300 nm, particularly preferably 240 nm to 280 nm, via the pump pressure of the first counter jet disperser, and also the proportion of drops with a diameter, in particular average diameter,> 1 pm, in particular from 1 pm to 50 pm, significantly and in particular reproducibly reduced, via the pump pressure of the second Schmidtstrahldispergators.
• the first counter jet disperser can be operated at a pump pressure of 1900 bar and the second counter jet disperser at a pump pressure of 500 bar.
• the first Jacobstrahldispergator at a pump pressure of 1500 bar and the second Jacobstrahldispergator be operated at a pump pressure of 500 bar.
• the first Jacobidian at a pump pressure of 1200 bar and the second Jacobstrahldispergator be operated at a pump pressure of 500 bar.
• first counter jet disperser and the second counter jet disperser may each be operated at a same temperature of the O / W preemulsion.
• both the first counter jet disperser and the second counter jet disperser may be operated at a 50 ° C O / W preemulsion temperature.
• the at least one may be downstream of a pressure reducer.
• the pressure reducer is preferably configured to generate a backpressure to a pressure generated by the at least one counter jet disperser, in particular pump pressure.
• the pressure reducer may be adapted to generate a back pressure of 10 bar to 100 bar, in particular 30 bar to 70 bar.
• a droplet diameter in particular average droplet diameter (determined by photon correlation spectroscopy, PCS)
• PCS photon correlation spectroscopy
• an O / W emulsion having a pFAT5 value of 0.001% to 0.01% can be produced by means of the process according to the invention.
• a parenterally administered O / W emulsion is prepared by the method according to the invention.
• the invention relates to an oil-in-water emulsion, hereinafter abbreviated as O / W emulsion, which is prepared or preparable by a process according to the first aspect of the invention.
• the invention according to a second aspect relates to an oil-in-water emulsion, hereinafter abbreviated as O / W emulsion, which has a pFAT5 value ⁇ 0.04%, in particular ⁇ 0.03%, preferably ⁇ 0 , 02%, more preferably ⁇ 0.01%, in particular ⁇ 0.01%.
• O / W emulsion may have a pFAT5 value of 0.001% to 0.01%.
• the O / W emulsion has a drop diameter, in particular average drop diameter (determined by photon correlation spectroscopy, PCS), from 180 nm to 340 nm, in particular 200 nm to 320 nm, preferably 200 nm to 300 nm, particularly preferably 240 nm to 280 nm.
• a drop diameter in particular average drop diameter (determined by photon correlation spectroscopy, PCS)
• PCS photon correlation spectroscopy
• the invention relates to a plant for producing an oil-in-water emulsion, hereinafter abbreviated as O / W emulsion, and / or for carrying out a process according to the first aspect of the invention.
• the plant has at least one pre-mix disperser, i. Prehomogenizing or pre-emulsifying, an oil phase and a water phase to an oil-in-water pre-emulsion (hereinafter abbreviated as O / W pre-emulsion), and at least one preferably downstream jet disperser for homogenizing the O / W Preemulsion to an oil-in-water emulsion, hereinafter abbreviated as O / W emulsion, on.
• pre-mix disperser i. Prehomogenizing or pre-emulsifying, an oil phase and a water phase to an oil-in-water pre-emulsion (hereinafter abbreviated as O / W pre-emulsion), and at least one preferably downstream jet disperser for homogenizing the O / W Preemulsion to an oil-in-water emulsion, hereinafter abbreviated as O / W emulsion, on.
• the at least one dispersant (for premixing the O / W preemulsion) is preferably designed as a rotor-stator-disperser, in particular rotor-stator.
• the system may comprise a rotor-stator-disperser or a plurality of rotor-stator-dispersers, ie several rotor-stator-dispersers, such as two, three, four or five, rotor-stator-dispersers.
• the system may comprise a plurality of parallel-connected rotor-stator dispersers and / or a plurality of rotor-stator dispersers connected in series.
• the plant may comprise a counter jet disperser or a plurality of counter jet dispersants, i. several counter jet dispersers, such as two, three, four or five Jacobstrahldispergatoren exhibit.
• the system may comprise a plurality of parallel jet counter-jet dispersers and / or a plurality of counter-jet jet dispersers connected in series.
• the plant preferably has at least two counter jet dispersers connected in series.
• an intermediate container can be connected between the at least one disperser (for premixing the O / W pre-emulsion) and the at least one counter jet disperser.
• the intermediate container facilitates with particular advantage by buffering the process flow, the coordination between the at least one rotor-stator-disperser and the at least one Gegenstrahldispergator.
• FIG. 4 shows a further flow chart of a method according to the invention.
• the channel structure 1 shown has a Y-shaped arrangement and may for example have an inner diameter d in the micrometer range.
• an O / W preemulsion can be passed through the channel structure 1 by means of a pressure generated by a pump (high pressure pump) of the counter jet disperser. Due to the oppositely disposed channels 4 and 6, jets of the O / W preemulsion collide in a drop comminution zone 5. In particular under the influence of shear forces, comminution of drops contained in the O / W preemulsion occurs there. The resulting O / W emulsion can leave the channel structure 1 via an outlet 7.
• Fig. 2 shows schematically a flow chart of a method according to the English method.
• a pre-disperser 10 with a rotor-stator system 11 is used.
• WFI water for injection
• the water may also be admixed with a stabilizer or isotonizing additive, such as, for example, glycerol, and with an emulsifying aid, such as, for example, sodium oleate.
• the mixture can be heated or tempered for example over a period of 60 minutes to a temperature of 55 ° C to 75 ° C.
• an oil phase can take place in a container 20, which can be designed as a pre-tempering container, with a stirring element 21.
• a container 20 which can be designed as a pre-tempering container, with a stirring element 21.
• soybean oil and medium-chain triglycerides (MCT) and a-tocopherol can be used to provide the oil phase.
• MCT medium-chain triglycerides
• the mixture produced in the container 20 can also be heated or tempered to a temperature of for example 55 ° C to 75 ° C.
• the oil phase and water phase provided in this way are then fed into a rotor-stator disperser 30.
• the oil phase and the water phase are preferably spatially separated from each other fed into the rotor-stator-disperser 30. This can be done, for example, by means of a coaxial tube or a coaxial tube. This can ensure that the oil drops are exposed to a sufficient emulsifier concentration.
• the oil phase and the water phase are preferably conducted through a shearing zone 32 of the rotor-stator disperser 30.
• a shearing zone 32 of the rotor-stator disperser 30 As a result, an effective comminution of oil droplets with a diameter, in particular average diameter,> 1 pm can already be achieved at this process stage.
• premixing of the oil phase and the water phase to an O / W preemulsion occurs.
• the O / W preemulsion can be fed via a buffer 40 to at least one counter jet disperser 50.
• the buffer or container is used with particular advantage to maintain the process flow and thus facilitates the coordination between the rotor-stator-disperser 30 and the at least one Jacobstrahldispergator 50th
• the counter jet disperser 50 is operated by means of a high pressure pump, which in particular can generate a pressure in the range from 500 bar to 1900 bar.
• a high pressure pump which in particular can generate a pressure in the range from 500 bar to 1900 bar.
• the pump pressure generated within the counter jet disperser 50 the O / W preemulsion is pumped through a microchannel structure having preferably opposite channels. At this time, jets of the O / W preemulsion in the drop comminution zone meet, whereby drops contained in the O / W preemulsion are crushed, especially under the action of shear forces.
• droplets can be produced with particular advantage which have a diameter, in particular average diameter (determined by photon correlation spectroscopy, PCS), from 180 nm to 340 nm, in particular 200 nm to 320 nm, preferably 240 nm to 280 nm.
• PCS photon correlation spectroscopy
• the O / W emulsion produced in the counter jet disperser 50 can then be transferred to a filling container 70 for further filling in suitable packaging sizes.
• Fig. 3 shows schematically another flow diagram of a method according to the invention, which is operated by the English method.
• the illustrated method differs from the method illustrated in FIG. 1 in that it is operated with two counter jet dispersers 50 and 60 connected in series.
• the first counter jet disperser 50 preferably drops with a diameter, in particular average diameter (determined by photon correlation spectroscopy, PCS), of 180 nm to 340 nm, in particular 200 nm to 320 nm, preferably 200 nm to 300 nm, particularly preferably 240 nm to 280 nm, while in the second, d. H. downstream, Jacobstrahldispergator 60 preferably a reduction of the proportion of drops with a diameter, in particular average diameter, of> 1 pm, and thus takes place a reduction of the pFAT5 value.
• PCS photon correlation spectroscopy
• the first counter jet disperser 50 can be operated, for example, at a pump pressure of 1500 bar, wherein the O / W preemulsion within the counter jet disperser 50 preferably has a temperature of 50 ° C.
• the second Jacobstrahldispergator 60 is preferably operated at a pump pressure of 500 bar, wherein the O / W emulsion within the Gegenstrahldispergators 60 preferably has a temperature of 50 ° C.
• FIG. 4 shows schematically a further flowchart of a method according to the invention. In this case, however, the method is based on the continental method.
• a water phase is provided by means of a container 15, which may be designed as Vortemperier disposer, and the oil phase by means of a pre-disperser 25 with a rotor-stator system 23 is provided.
• water in particular water for injection purposes (WFI), for example, mixed with sodium hydroxide solution and glycerol and the resulting mixture with stirring by means of a stirrer element 13, for example, heated to a temperature of 55 ° C to 75 ° C or tempered.
• WFI water for injection purposes
• oil phase for example, oleic acid, soybean oil and medium chain triglycerides with an emulsifier, such as egg lecithin, and an antioxidant, such as a-tocopherol, and the resulting mixture also with stirring to a temperature of 55 ° C to 75 ° C. heated or tempered.
• the method sequence and the reference numbers correspond to the method sequence shown in FIG. 2 as well as the reference numbers shown in FIG.
• the manufacturing process was divided into the following three process steps.
• the production of the oil phase and water phase took place.
• the water phase was prepared in a stirred tank reactor for crushing and dissolving the emulsifier.
• the preparation of the oil phase was carried out by simple temperature control of the oil phase on a magnetic stirrer.
• preparing an O / W-pre-emulsion was made by means of a dispersant under the designation ULTRA-TURRAX ® Inline (Ytron-Z) commercially available rotor-stator.
• ULTRA-TURRAX ® Inline Ytron-Z
• the oil phase and the water phase were guided by means of a forced passage through the shear zone of the rotor-stator disperser. This ensured that every part of the oil phase also passed through the homogenization zone.
• the introduction of the oil phase into the rotor-stator-stirrer can only be considered statistically and, according to experience, leads to an undesirably broad and only partially controllable particle distribution.
• the final fine emulsion was prepared by means of a PSI-40 high pressure homogenizer designed as a counter jet disperser.
• a PSI-40 high pressure homogenizer designed as a counter jet disperser.
• the counter jet disperser had a static microchannel structure for droplet breakup.
• the used rotor-stator-disperser (Ytron-Z) consisted of eleven main components.
• the raw materials oil phase and water phase
• two feed funnels which could each be closed or opened via a disk valve.
• the raw materials flowed directly into the inlet of two diaphragm motor metering pumps (ProMinent ® Sigma / 1 control type S1 Cb).
• These two pumps operated on the principle of an oscillating positive displacement pump, which were driven by an electric motor. This transmitted by means of a push rod a lifting movement on a dosing membrane.
• the stroke movement of the displacer was continuously recorded and regulated, so that the stroke could be carried out according to a predetermined metering profile and thus could be adapted accordingly to the properties of the raw materials (viscosity and / or outgassing property).
• the metering was carried out via a metering head with a tube-in-tube structure. While the oil phase was centered through the inner tube, the water phase was passed in a surrounding outer tube.
• the raw materials were pumped by means of the two metering pumps directly into a reactor head and ran there by means of a forced passage directly into a rotating rotor / stator set. This was driven by means of a three-phase motor (ATB Motorenwerke GmbH, IM B3, 1, 5 kW).
• KVT GmbH a pressure air driven guetsch valve
• the gate valve served as a technically obligatory backpressure valve for the correct functionality of the two diaphragm metering pumps, as well as a reduction unit of the product outlet, to ensure that the reactor head reached its working volume and could not run empty in the process.
• the system was controlled via a control cabinet by means of a programmable logic controller (PLC, SIMATIC, Siemens AG).
• PLC programmable logic controller
• the proportions of the two metering pumps and the speed of the rotor-stator disperser could be entered via a touch panel mounted in the control cabinet door and started simultaneously.
• the shaft of the rotor-stator disperser was sealed by means of a product-lubricated mechanical seal.
• the rotor disk was stretched by means of a key on the rotary shaft of the three-phase motor and was fixed by means of a rotor screw with an O-ring seal on this.
• the stator was bolted firmly to the reactor lid and was displaced contactlessly against the rotor disk when the reactor head was closed.
• the reactor head was closed by a clamp connection with an O-ring seal.
• Table 1 Formulation of a model emulsion (parenteral fat emulsion)
• the preparation of the water phase was carried out in a 10 l stirred tank, which was tempered by means of a tempering unit via a double jacket to 65 ° C process temperature.
• This process step essentially served the comminution and hydration of the emulsifier in the water phase.
• egg lecithin (emulsifier), glycerol and sodium oleate were placed in a stirred tank and filled with tempered (65 ° C) water for injections (Wfl) to a volume of 10 I.
• soybean oil To prepare the oil phase soybean oil, MCT and alpha-tocopherol were added to a beaker and then, heated to a process temperature of 75 ° C on a magnetic stirrer, preparatory to use in-line ULTRA-TURRAX ® and in a second receiving vessel of the inline rotor Stator reactor transferred. This reservoir also had a jacket temperature, which tempered the oil phase during the emulsification to process temperature. The preparation of the oil phase was completed with this step.
• a rotor with a slot width of 1 mm and a stirrer circumference of 33 mm was used for an innermost sprocket, a stirrer circumference of 44 mm for a middle sprocket and a stirrer circumference of 55 mm for an outer sprocket.
• the tooth spacing of the stator was 0.5 mm.
• the circumference of the three sprockets was 38 mm for an inner sprocket, 49 mm for a middle sprocket and 60 mm for an outer sprocket.
• the pressure at the product outlet was set to a back pressure of 2 bar.
• the O / W pre-emulsion was collected at the product outlet in a beaker while constantly stirring.
• the O / W emulsion was finely emulsified in a three-pass PSI-40 type high-pressure homogenizer designed as a counter jet disperser.
• this high-pressure homogenizer used a static micrometer-sized channel structure in which the droplet break-up took place. Due to the much narrower and unchangeable channel dimension, a more intensive shear and a lower and reproducible flow distribution with resulting narrow droplet distributions took place. Furthermore, such high pressure homogenizers are easier to scale due to their static chamber geometry. Drop breakage took place in an interaction chamber (shear chamber) consisting of a diamond core buried in a 316L stainless steel jacket.
• the diamond core was designed with the above-mentioned microstructured channels in which the drops were accelerated and broken at high process pressure.
• so-called Y-chambers were used.
• the microchannels formed the shape of a wye in such chambers. In this case, process pressures of 500 bar to 2,000 bar were possible.
• the interaction chamber was followed by an APM (auxiliary processing module) (secondary chamber).
• APM auxiliary processing module
• This secondary chamber acted as a pressure reducer and produced a low back pressure on the outlet side (outlet) of the primary chamber.
• a relaxation of the interaction chamber against the direct atmospheric pressure with induced cavitation was so prevented.
• the APM module was a stainless steel core with a specially dimensioned bore in a stainless steel jacket.
• the chamber E101 D was a single-slot Y-chamber and delivered flow rates up to 20 L / h.
• the APM module delivered a back pressure of about 50 bar for the primary chamber E101 D.
• the chamber E101 D was a single-slot Y-chamber and delivered flow rates up to 20 L / h.
• the APM module (reduced backpressure) provided backpressure for the primary chamber E101 D, but with a reduced backpressure near 50 bar.
• the information regarding the generated back pressures was based on manufacturer information.
• PCS Photon Correlation Spectroscopy
• the Brownian motion is quantified with the aid of an autocorrelation function of the scattered light signal of disperse particles.
• a light beam with a defined wavelength is passed through a sample by means of a laser, which results in a scattering of the laser light.
• the scattered light intensity is subject to time-dependent fluctuations due to the non-directional diffusion of molecules surrounding the particles. These time-dependent interference phenomena depend on the size of the scattering particles.
• the microimage was led with the unit [drop].
• the microimage corresponded to the number of drops of five image samples of a considered sample volume.
• the fat emulsion prepared according to 1 was prepared using various homogenizing temperatures and pressures.
• a PSI-40 counter jet disperser was used. From a description of the company Microfluidics (Chamber User Guide, 12/30/14) is known how the process temperature changes with the pressure during homogenization (2.5 ° C per 100 bar). This temperature is to be added to the respective test temperature T H of the O / W preemulsion, ie the temperature of the O / W preemulsion before it enters the at least one counter jet disperser, and gives the homogenization temperature for the purposes of the present invention. For example, for an O / W preemulsion which has a temperature of 20 ° C.
• a temperature of O / O is calculated for a counter jet disperser which is operated at a homogenization pressure (pump pressure) of 1000 bar. W preemulsion within the counter jet disperser of 45 ° C.
• the test results obtained show that drops having a diameter, in particular average diameter, above 1 pm, in particular between 1 pm and 5 pm, preferably at a homogenization pressure below 1000 bar, in particular at a homogenization pressure of 500 bar, are comminuted.
• both the targeted in relation meets the minimum standard existing on the mean droplet diameter as well as the minimum standard assumed in relation to the pFAT5 value, and consequently the process quality is significantly increased.
• the fat emulsion prepared according to 1. was prepared using two series-connected counter jet dispersers (each of type PSI-40). The results obtained are shown in the following Tables 1 1 to 13.
• the tabulated results show that the minimum medical standard required for parenterally administered O / W emulsions in terms of mean drop diameter is met by all O / W emulsions produced. Furthermore, the results show that the average droplet diameter can be additionally reduced by the use of a second series-connected counter jet disperser. If the second counter jet disperser is also at a homogenizing pressure (pump pressure) ⁇ 1000 bar, operated in particular at a homogenization pressure of 500 bar, the pFAT5 value valid for parenterally administered O / W emulsions can be clearly undershot. Overall, therefore, a significant increase in the process quality, in particular with respect to the mean droplet diameter and the pFAT5 value of the O / W emulsions to be produced, can be achieved.

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