EP3638411B1 - Procédé et dispositif de mélange pour la régulation de l'introduction d'une substance sous forme de poudre dans un liquide pour un procédé de mélange en ligne - Google Patents

Procédé et dispositif de mélange pour la régulation de l'introduction d'une substance sous forme de poudre dans un liquide pour un procédé de mélange en ligne Download PDF

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Publication number
EP3638411B1
EP3638411B1 EP18718687.9A EP18718687A EP3638411B1 EP 3638411 B1 EP3638411 B1 EP 3638411B1 EP 18718687 A EP18718687 A EP 18718687A EP 3638411 B1 EP3638411 B1 EP 3638411B1
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EP
European Patent Office
Prior art keywords
time
dependent
current consumption
mixed product
duration
Prior art date
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EP18718687.9A
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German (de)
English (en)
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EP3638411A1 (fr
Inventor
Uwe Schwenzow
Erwin Süthold
Ludger Tacke
Mikkel Mork Nielsen
Claus Patscheider
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GEA TDS GmbH
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GEA TDS GmbH
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Priority claimed from DE102017005573.4A external-priority patent/DE102017005573B3/de
Priority claimed from DE102017005574.2A external-priority patent/DE102017005574B3/de
Application filed by GEA TDS GmbH filed Critical GEA TDS GmbH
Priority to PL18718687T priority Critical patent/PL3638411T3/pl
Publication of EP3638411A1 publication Critical patent/EP3638411A1/fr
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    • 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
    • B01F23/50—Mixing liquids with solids
    • B01F23/51—Methods thereof
    • 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
    • B01F23/50—Mixing liquids with solids
    • B01F23/53—Mixing liquids with solids using driven stirrers
    • 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
    • B01F23/50—Mixing liquids with solids
    • B01F23/59—Mixing systems, i.e. flow charts or diagrams
    • 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
    • B01F25/50—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle
    • 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
    • B01F27/23—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis
    • B01F27/232—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis with two or more rotation axes
    • B01F27/2321—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis with two or more rotation axes having different inclinations, e.g. non parallel
    • 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
    • B01F27/60—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis
    • B01F27/61—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis about an inclined axis
    • 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
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms 
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/20—Measuring; Control or regulation
    • B01F35/21—Measuring
    • B01F35/212—Measuring of the driving system data, e.g. torque, speed or power data
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/20—Measuring; Control or regulation
    • B01F35/22—Control or regulation
    • B01F35/2201—Control or regulation characterised by the type of control technique used
    • B01F35/2209—Controlling the mixing process as a whole, i.e. involving a complete monitoring and controlling of the mixing process during the whole mixing cycle
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/20—Measuring; Control or regulation
    • B01F35/22—Control or regulation
    • B01F35/221—Control or regulation of operational parameters, e.g. level of material in the mixer, temperature or pressure
    • B01F35/2216—Time, i.e. duration, of at least one parameter during the operation
    • B01F35/22162—Time of feeding of at least one of the components to be mixed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/71—Feed mechanisms
    • B01F35/717—Feed mechanisms characterised by the means for feeding the components to the mixer
    • B01F35/71755—Feed mechanisms characterised by the means for feeding the components to the mixer using means for feeding components in a pulsating or intermittent manner

Definitions

  • the invention relates to a first method for controlling the introduction of a powdery substance into a liquid consisting of at least one component for an inline mixing process according to independent claim 1 and a corresponding second method according to the preamble of independent claim 2, in which the introduction and treatment of the powdery Substance takes place under the reaction kinetic conditions of a residence time behavior of a continuously operating homogeneous reaction vessel, as well as a mixing device for carrying out the respective process.
  • mixer technology With a view to the introduction of a powdery substance into a liquid and its uniform distribution and, if necessary, dissolution in the liquid, mixer technology knows mixing processes that are operated intermittently (so-called batch process) or continuously (so-called inline process).
  • the mixing of liquid and powdery substance is carried out kinetically in a so-called discontinuously operated reaction vessel (mixing vessel).
  • a certain amount of liquid is placed in the mixing container and powdery substance is added until a desired or systematically predetermined dry substance concentration of the powdery substance is present in the liquid.
  • Powdered substance and liquid are preferably continuously stirred and / or mixed to form a mixed product and the mixed product is homogenized with the aim of uniformly distributing the powdery substance.
  • the powdery substance can be fed in continuously or discontinuously.
  • a mixed product produced in a first phase and corresponding to the single-pass process is recirculated through the mixing container in a second phase, with pulverulent material still being fed in either continuously or discontinuously.
  • the mixed product is recirculated until it has a dry matter concentration that has grown to a predetermined end value.
  • various forms of the method are known which provide that the entire mixed product discharged from the mixing container is either passed directly through the mixing process again or first passed through a storage volume and then likewise fed back into the mixing process. Any distribution ratios can be implemented between these two forms.
  • the present invention deals exclusively with mixing processes which are operated in the inline process and here in all possible forms (single pass and any variants of the multiple pass process).
  • Mixing methods in this regard and the associated mixing devices were made known to the public, for example, at the following Internet link: "http://www.gea.com/de/products/High-Shear-Inline-Mixer.jsp”.
  • the U.S. 3,425,667 A describes a one-pass process for the continuous, controlled mixing of pigments and fillers with binder solutions or other liquids, in which solid and liquid components are in a controlled manner Quantities fed into a flow mixer and mixed there with one another.
  • the control involves measuring the ratio of liquid and solid components in the mixture after the mixture has passed through the flow mixer.
  • the regulation of the supply of liquid takes place as a function of this measurement, the regulation of the supply of solids comprising separate control means.
  • the above-mentioned mixing devices preferably also include so-called vacuum mixers, which have a mixing container with a stirring and / or shearing and homogenizing device.
  • the free surface of the liquid, which in the mixing container can, for example, have a free fill level with a height of between 0.4 and 4 m, is subject to a negative pressure corresponding to this height range compared to atmospheric pressure of, for example, 0.2 to 0.8 bar, so that the Liquid can on the one hand be freed from gas components more easily during the mixing process and on the other hand has a negative pressure compared to atmospheric pressure in the bottom area of the mixing container under all operating conditions.
  • the powdery substance is introduced into the mixing container via an opening in the container wall below the free fill level.
  • This opening continues in a tubular inlet connection in the direction of the outside of the mixing container, to which a pipeline leading, for example, to a powder storage container is connected.
  • the inlet nozzle and thus the pipeline can be shut off via an inlet valve that controls the supply of the powdery substance, so that, on the one hand, the mixing device is closed off from its surroundings via this path and, on the other hand, an amount of the powdery substance in the powder storage container is automatically fed to the liquid if necessary due to the prevailing pressure conditions can be.
  • a related mixing device with a preferably discontinuous supply of the powdery substance is in the document DE 10 2015 016 766 A1 described.
  • a discontinuous supply of the powdery substance as for example in the DE 10 2015 016 766 A is disclosed, has the advantage that the supply always takes place via the fully open position of the inlet valve designed as a lift valve and thereby the risk of clogging of the inlet valve is minimized.
  • Addicted from the duration of the respective open position more or less large amounts of the powdery substance are introduced into the liquid in bursts, so that there is basically the risk that there will be corresponding agglomerations of the powdery substance, which are caused by the stirring and / or shearing and homogenizing
  • the device must be completely dissolved until the subsequent entry of powdery substance, while at the same time striving for as uniform a distribution of the powdery substance as possible.
  • the object of the present invention is to develop two generic methods for controlling the introduction of a powdery substance into a liquid consisting of at least one component for an inline mixing process and associated mixing devices for carrying out the respective process in such a way that the above-mentioned disadvantages of the prior art be eliminated.
  • this object is achieved by a first method with the features of independent claim 1 and by a second method with the features of independent claim 2. Furthermore, the object is achieved in terms of device technology by a mixing device for performing the respective method with the features of claims 12 and 13, respectively.
  • the invention is based on a method for controlling the introduction of a powdery substance into a liquid consisting of at least one component for an inline mixing method, where the term “component” is to be understood in such a way that it can generally involve discrete liquids that are separate from one another and that can also be fed to the mixing process separately from one another.
  • This first process a so-called single-pass process or a single-stage process, is typically used for the production of low-viscosity base sludge with a low dry matter concentration or, for example, for skimmed milk powder in water or cocoa powder in milk or, more generally, when a powdery substance with good solubility in needs to be resolved in a short time.
  • the introduction and treatment of the pulverulent substance takes place under the conditions of a residence time behavior of a continuously operating homogeneous reaction vessel, namely in such a way that the liquid is fed continuously and the pulverulent substance discontinuously to a mixing container, the goal being a predetermined time constant dry matter concentration of the powdery substance in the liquid.
  • the liquid and the powdery substance are continuously stirred and / or mixed to form a mixed product and the mixed product is homogenized.
  • the treatment processes “stirring”, in which no or only a very low mechanical force is applied to the mixed product, and “mixing”, in which a significant shear force is applied to the mixed product and therefore the “mixing” in this regard as well is classified as “shearing”, with “homogenizing” mostly being an integral part of mixing.
  • the mixed product is continuously discharged according to the added amounts of liquid and powdery substance.
  • a recipe for the mixed product is given, at least with regard to the given dry matter concentration, and the reaction conditions are given in each case in the form of default data.
  • the reaction conditions provide that the powdery substance is sucked in by a negative pressure (vacuum) in the head space of the mixing container compared to atmospheric pressure.
  • the dosing pulses are each caused by a mass flow of the powdery substance ⁇ P , a duration of the dosing pulse ⁇ t1 and a time interval between adjacent dosing pulses ⁇ t2.
  • a significant technical control feature is that a time-dependent current consumption I (t) is determined, which is proportional to the stirring and / or shearing and homogenizing power required for a temporarily present mixed product.
  • I (t) is determined, which is proportional to the stirring and / or shearing and homogenizing power required for a temporarily present mixed product.
  • the latter always occurs approximately in the form of a Gaussian normal distribution when a defined amount of powdery substance m P is introduced into the mixing process or the mixing container and treated in pulses.
  • the time-dependent current consumption I (t) subsides, to a reference current consumption I o , which is characteristic of the completely homogenized mixed product performing stirring and / or shearing and homogenizing performance.
  • the relevant reference current consumption I o is stored in the default data and can be used from there, and it depends on the recipe of the mixed product and the reaction conditions for the mixing process.
  • the core of the control measure according to the invention is that the duration of the dosing pulse ⁇ t1 and the time interval between adjacent metering pulses ⁇ t2 are selected in such a way that at the end of the time interval between adjacent metering pulses ⁇ t2, the time-dependent current consumption I (t) for stirring and / or shearing is determined and homogenizing the temporarily present mixed product approximates the reference current consumption I o , which is required for the relevant treatment of the homogenized mixed product, within the scope of a practically relevant permissible tolerance.
  • the invention is based on a known method for controlling the introduction of a powdery substance into a liquid consisting of at least one component for an inline mixing method, which is also classified as a multi-pass method or multi-stage process.
  • the multi-pass process is typically used for mixed products that ultimately have a higher dry matter concentration and / or a higher viscosity, for example when larger amounts of powdery substance have to be emulsified, for example with oil, gum or aromas, because these mixed products with the single pass procieedings cannot be represented.
  • the introduction and treatment of the pulverulent substance, from a reaction kinetic point of view takes place again, as in the first method, under the conditions of a residence time behavior of a continuously operating homogeneous reaction vessel.
  • the second method is characterized in a manner known per se in such a way that in a first phase liquid is placed in a mixing container and the powdery substance is fed discontinuously to this liquid, with a dry substance concentration being reached at the end of the first phase that is below one for the The end value specified at the end of the entire mixing process is.
  • the liquid and the powdery substance are continuously stirred and / or mixed into a mixed product in the first phase and the mixed product is homogenized.
  • the mixed product obtained in the first phase is recirculated via the mixing container and quantities of pulverulent material corresponding to the recirculated amount of mixed product are also added discontinuously.
  • the quantity balance is accordingly designed in the second phase at a constant fill level according to the continuity condition in such a way that the mass flow of mixed product discharged from the mixing process corresponds to the mass flow of mixed product routed via the recirculation plus the dosed mass flow of powdery substance.
  • the mixed product is recirculated until a time-dependent course of a dry matter concentration of the powdery substance in the mixed product has grown to a predetermined end value.
  • a recipe for the mixed product is given, at least with regard to the time-dependent curve of a dry matter concentration associated with the given end value, and the reaction conditions are given in the form of default data.
  • the inventive solution concept consists in the second method that the discontinuous supply of the pulverulent substance in a manner known per se takes place in pulses by a chronological sequence of metering pulses.
  • the reaction conditions provide, in a preferred embodiment and in line with the first method, that the powdery substance is sucked in by a negative pressure (vacuum) in the head space of the mixing container compared to atmospheric pressure.
  • the metering pulses are each characterized by a mass flow of the powdery substance ⁇ P , a duration of the metering pulse ⁇ t1 and a time interval between adjacent metering pulses ⁇ t2.
  • a significant technical control feature is that a time-dependent current consumption I (t) is determined, which is proportional to the stirring and / or shearing and homogenizing power required for a temporarily present mixed product.
  • I (t) is determined, which is proportional to the stirring and / or shearing and homogenizing power required for a temporarily present mixed product.
  • the latter always occurs in the form of an approximately Gaussian normal distribution when a defined amount of powder Substance is introduced and treated in pulses in the mixing process or the mixing container.
  • the time-dependent current consumption I (t) subsides, namely on a time-dependent course a reference current consumption I o (t), which is characteristic of the stirring and / or shearing and homogenizing power to be provided on the homogenized mixed product under the conditions of the assigned time-dependent curve of a dry matter concentration c (t).
  • the related course of a reference current consumption I o (t) is stored in the specification data and can be drawn from there, and it depends on the recipe of the mixed product and the reaction conditions for the mixing process.
  • the duration of the dosing pulse ⁇ t1 for the subsequent dosing pulse is shortened in the first case and lengthened in the second case.
  • This technical control measure with a variable duration-time interval ratio V requires the control to be able to shorten or lengthen the duration of the metering pulse ⁇ t1 with an unchanging time interval between adjacent metering pulses ⁇ t2 or to adequately lengthen the time interval between adjacent metering pulses ⁇ t2 with the same duration of the metering pulse ⁇ t1 or shorten it.
  • the control-technical measure according to the invention therefore essentially consists in both embodiments of the second method in that the duration of the metering pulse ⁇ t1 and the time interval between adjacent metering pulses ⁇ t2 are selected in such a way that at the respective end of the time interval between adjacent metering pulses ⁇ t2 the time-dependent determined current consumption I (t) for stirring and / or shearing and homogenizing the temporarily present mixed product approximates the time-dependent course of a reference current consumption I o (t), which is required for the relevant treatment of the homogenized mixed product, within the scope of a practically relevant permissible tolerance.
  • the second method which is primarily suitable for increasing the dry matter concentration to a predetermined final value, provides that the recirculated mixed product is divided into a first portion and a second portion, that the first portion is fed directly to the mixing process and that the complementary second portion is guided over a storage volume and then also fed to the mixing process.
  • This division offers the possibility, as is proposed, of setting the first portion recirculated directly via the mixing process between zero and one hundred percent of the recirculated mixed product.
  • Such a configuration and mode of operation offers the possibility of concentrating smaller amounts of the desired mixed product exclusively in the mixing container with the maximum possible first proportion (100%).
  • the mass flow of the pulverulent substance is constant over the duration of the metering pulse. This is ensured in particular by the fact that a controllable opening for the supply of the powdery substance only assumes either a fully open position or a closed position.
  • a different embodiment for both methods provides that the shortening or lengthening of the duration of the metering pulse takes place when a current corridor determined by a permissible current overrun or a permissible undercurrent through an upward deviating current corridor Current consumption or a current consumption deviating downwards is left.
  • the permissible current excess and the permissible current shortfall are each represented by a percentage of the assigned reference current consumption or the assigned time-dependent course of a reference current consumption is determined.
  • the degree of shortening or lengthening of the duration of the metering pulse is determined as a function of the degree of deviation of the time-dependent current consumption from the assigned reference current consumption or the assigned time-dependent course of a reference current consumption.
  • control of the introduction of the powdery substance into the at least one liquid is based on further recipe-dependent default data from empirical values previous mixing processes are obtained and stored, these default data being a flow rate of the at least one liquid, a mixing or solution temperature (reaction temperature), a pressure above the liquid column from which a reaction pressure results, speeds of devices for stirring and / or shearing and homogenizing and a permissible current exceedance and a permissible current undercurrent are dependent on the assigned reference current consumption or the assigned time-dependent course of a reference current consumption.
  • reaction temperature mixing or solution temperature
  • a further embodiment provides for both methods that the target-oriented recipe-dependent control parameters obtained in the course of the control of the introduction of the powdery substance into the at least one liquid, namely the duration of the metering pulse and the time interval between adjacent metering pulses, stored and used for subsequent controls of the same recipes.
  • a mixing device for carrying out the first method consists in a manner known per se of a mixing container which has an inlet connection for the supply for a liquid, an outlet nozzle for discharging a mixed product and a stirring device and / or a shearing and homogenizing device.
  • An inlet valve with a valve closing member is arranged on the mixing container. The inlet valve can be adjusted with the valve closing element either between completely closed (closed position) or completely open (open position). A powdery substance is introduced into the liquid with the inlet valve, with the valve closing element being able to be moved into the closed or open position with a control device assigned to the inlet valve.
  • the control device of the mixing device provides recipe-dependent specification data and recipe-dependent control parameters in the form of the duration of the metering pulse and the time interval between adjacent metering pulses. Furthermore, according to the invention, the control device has at least one signal pickup designed as a measuring device, which detects a time-dependent current consumption of the stirring device and / or the shearing and homogenizing device. Equipped with these properties, the control device controls the closed or open position of the valve closing element as a function of the time-dependent power consumption and in relation to the specified data and the control parameters.
  • a mixing device for carrying out the second method is constructed essentially adequately to the mixing device for carrying out the first method.
  • the difference results from the task on which the second method is based, to achieve the greatest possible concentration of small to large amounts of mixed product with powdery substance by recirculating the mixed product.
  • a structural addition to the mixing device is provided in the form of a circulation line, which branches off from a line connected to the outlet connection and opens directly into the mixing container.
  • an advantageous embodiment provides that the valve closing member is designed, at least in its powder-loaded area, as a cylindrical rod of the same diameter, on which a valve disk is molded with the same diameter.
  • the valve closing member with its valve disk is largely moved out of the fully developed flow of the powdery substance due to this embodiment, so that on the one hand it does not represent a flow obstacle and on the other hand there is a seat seal that is accommodated in the valve disk the vicinity of the wall of a valve housing and thus outside the fully developed flow area of the pipe flow and is therefore only affected by the stagnant flow close to the wall in this edge area.
  • a mixing device 1000 has, inter alia, a mixing container 100 which consists of a preferably cylindrical container jacket 100.1, an upper container base 100.2 and a lower container base 100.3.
  • the lower container bottom 100.3 preferably tapers downwards, mostly conically or in the form of a circular cone, and at the lower end has an outlet connection 100.4 for a mixed product M, which is discharged with a mass flow of mixed product ⁇ M.
  • a liquid F with a flow rate of liquid ⁇ F is continuously fed to the mixing container 100 via an inlet connection 100.5, which forms a free fill level N above which, in the case of the mixing device 1000 in question (vacuum mixer), a pressure above the liquid column p, a negative pressure, is usually compared to atmospheric pressure, prevails.
  • An inlet valve 20 is arranged on the container jacket 100.1 or the lower container base 100.3.
  • the inlet valve 20 is used for the discontinuous supply of a powdery substance P with a mass flow of powdery substance ⁇ P , which is fed via a feed line 18, into the liquid F or into the mixed product M.
  • the inlet valve 20 is assigned a control device 30, which has a control head housing 14 of the inlet valve 20 communicates via a signal line 22 and, if necessary, the inlet valve 20 is transferred into its open or closed position.
  • a stirring device 24 driven by a first drive motor 40 at a rather low first speed n1, preferably arranged centrally and acting mechanically, which preferably extends down into the area of the lower container bottom 100.3.
  • the required stirring effect can also be achieved by fluid mechanical means, for example by pumping the liquid F or the mixed product M through an in Figure 1 circulation line, not shown, or one as in Figure 1a
  • the circulation line 28 shown having a comparable effect, with preferably tangential entry of the liquid F or the mixed product M into the mixing container 100, can be reached or supported.
  • a shearing and homogenizing device 26 driven by a second drive motor 50 with a rather high second speed n2 is preferably provided in the lower region of the lower container bottom 100.3 and preferably eccentrically in this. This preferably sucks in the liquid F on the one hand from above and on the other hand ejects it in the form of a ring in the area of the lower container bottom 100.3 close to the wall in such a way that a circulation flow directed from the outside inward is preferably formed in the mixing container 100.
  • liquid F and powdery substance P or the mixed product M resulting therefrom are mechanically mixed very intensively and preferably homogenized in the process.
  • the inlet valve 20 is designed as a lift valve ( Figure 2 ).
  • a valve housing 2 it has a valve seat 2a and a valve disk cooperating with it 8a, which is formed on a valve closing member 8.
  • the valve closing member 8 receives a seat seal 10, which in the closed position of the inlet valve 20, in cooperation with the valve seat 2a, effects the seal.
  • the valve seat 2a has a seat opening 2b through which the powdery substance P supplied from the supply line 18 via a pipe connection 2c is introduced into the liquid F ( Figure 1 ).
  • valve closing member 8 It is preferably a spring / piston drive acted upon by pressure medium, a return spring 12 usually moving the valve closing member 8 into its closed position when the drive housing 6 is not acted upon by pressure medium, preferably compressed air.
  • a valve rod 8b which engages the valve plate 8a of the valve closing element 8 and is guided through the drive housing 6 and into the control head housing 14, serves on the drive side for the axial guidance of the valve closing element 8.
  • the valve closing element 8 is at least in its powder-loaded area as a cylindrical rod of the same diameter formed on which the valve disk 8a is formed with the same diameter.
  • valve closing member 8 moving with it its end valve disk 8a and the associated seat seal 10 can be withdrawn as far as possible from the area of the valve housing 2 through which there is a full flow.
  • the control device 30 has at least one signal pickup 16.
  • the at least one signal sensor 16 is a measuring device, for example for mixing parameters, such as the volume flow of liquid ⁇ F , the pressure above the liquid column p in the mixing container 100, a mixing or solution temperature T of the liquid F, a dry matter concentration c or a time-dependent course of a Dry matter concentration c (t), speeds n1, n2 and a time-dependent current consumption I (t) of the stirring and / or shearing and homogenizing device 24, 26.
  • the signal pick-up 16 is shown in FIG Figure 1 shown by way of example for the time-dependent current consumption I (t) of the second drive motor 50 of the shearing and homogenizing device 26.
  • additional or alternatively further measuring devices can be provided which determine the other mixing parameters.
  • a mixing device 1000 for the second method differs from that for the first method only in that a circulation line 28 is provided, which branches off from a line connected to the outlet nozzle 100.4 and opens directly into the mixing container 100, preferably via its own recirculation connection 100.6 .
  • the line connected to the outlet connection 100.4 can be routed through one or more storage tanks and finally connected to the inlet connection 100.5.
  • the introduction and treatment of the pulverulent substance P takes place quasi under the reaction kinetic conditions of a residence time behavior of a continuously operating homogeneous reaction vessel.
  • the liquid F Via the inlet connection 100.5 with the flow rate of liquid ⁇ F , which in the most general case can be a time-dependent flow rate of liquid ( ⁇ F (t)), continuously and the powdery substance P via the inlet valve 20 discontinuously with the flow rate of powdery substance ⁇ P , which is in In the most general case, a time-dependent mass flow of powdery substance ( ⁇ P (t)) can also be fed to the mixing process in the mixing container 100, the goal being the predetermined, time-unchangeable dry matter concentration c of the powdery substance P in the liquid F.
  • the liquid F and the powdery substance P are continuously stirred and / or mixed to form the mixed product M and the mixed product M is homogenized in the process.
  • the mixed product M is continuously removed with the mixed product ⁇ M according to the supplied amounts of liquid F and powdery substance P.
  • a recipe for the mixed product M, at least with regard to the specified dry matter concentration c, and the reaction conditions in each case in the form of specified data D are specified.
  • the discontinuous supply of the powdery substance P takes place over a period of time t in pulses by a time sequence of metering pulses i ( Figures 3 and 4 ), which are each characterized by the mass flow of the powdery substance ⁇ P , a duration of the dosing pulse ⁇ t1 and a time interval between adjacent dosing pulses ⁇ t2.
  • Time-dependent current consumption I (t) plotted over the corresponding period t is determined or measured.
  • the latter is proportional to a stirring and / or shearing and homogenizing power required for a mixing product M * temporarily present in the mixing container 100 immediately after the dosing pulse i ( Figure 1 ), which is to be applied by the stirring and / or shearing and homogenizing device 24, 26 in this phase of the treatment.
  • the course of the time-dependent current consumption I (t) is similar to a Gaussian normal distribution curve, it increases with the intermittent flow of powdery substance ⁇ P , reaches a maximum, and then after dissolution of the powdery substance P, i.e. with a homogenized mixed product that is then reached M to gradually decrease to an initial value.
  • this typical behavior is used for control purposes in that a reference current consumption I o is used from the specification data D, which is characteristic of the stirring and / or shearing and homogenizing power to be provided on the homogenized mixed product M.
  • the tolerance consists of a specification of a permissible current exceedance ⁇ I1 and a permissible current undercurrent ⁇ I2 ( Figure 3 ).
  • the shortening or lengthening of the duration of the dosing pulse ⁇ t1 occurs when a current corridor determined by the permissible current exceedance ⁇ I1 or the permissible current undercurrent ⁇ I2 due to the time-dependent current consumption I * (t), I ** (t) deviating upwards or downwards. is left.
  • the permissible current excess and the permissible current shortfall ⁇ I1, ⁇ I2 are preferably each determined by a percentage of the assigned reference current consumption I o .
  • the amount of shortening or lengthening of the duration of the metering pulse ⁇ t1 is preferably determined as a function of the amount of deviation of the time-dependent current consumption I (t) from the assigned reference current consumption I o .
  • the permissible current excess ⁇ I1 and permissible current shortfall ⁇ I2 ultimately determined by the respective formulation of the mixed product M can be part of the specification data D for the mixing process.
  • recipe-dependent control parameters S namely the duration of the dosing pulse ⁇ t1 and the time interval between adjacent dosing pulses ⁇ t2, are stored and used for subsequent controls of the same recipes.
  • the control device 30 of the mixing device 100 is set up according to the invention so that it can provide the recipe-dependent default data D and the recipe-dependent control parameters S in the form of the duration of the metering pulse ⁇ t1 and the time interval between adjacent metering pulses ⁇ t2.
  • the control device 30 also has at least the signal pick-up 16 designed as a measuring device ( Figure 1 ), which records the time-dependent current consumption I (t) of the stirring device 24 and / or the shearing and homogenizing device 26 ( Figures 3, 4 ).
  • the control device 30 controls the closed or open position of the valve closing element 8 ( Figure 2 ) as a function of the time-dependent current consumption I (t) and in relation to the default data D and the control parameters S.
  • the introduction and treatment of the pulverulent substance P takes place under the reaction kinetic conditions of a residence time behavior of a continuously operating homogeneous reaction vessel.
  • liquid F is placed in the mixing container 100 (supply via the inlet connection 100.5) and the powdery substance P is fed to this total liquid F via the inlet valve 20 discontinuously with the mass flow of powdery substance ⁇ P , at the end of the first Phase a dry matter concentration c is reached, which is below a predetermined end value c E for the end of the entire mixing process.
  • the liquid F and the powdery substance P are continuously stirred by means of the stirring device 24 and / or mixed by means of the shearing and homogenizing device 26 to form the mixed product M and the mixed product M is homogenized.
  • the mixed product M obtained in the first phase is recirculated via the mixing container 100 and the recirculated product continues to be used Amount of mixed product M corresponding amounts of powdery substance P supplied discontinuously.
  • the amount of mixed product M discharged into the recirculation can be divided into a first portion a and a second portion b ((a + b) M).
  • the quantity balance is therefore compulsorily based on the continuity condition.
  • the mixed product M is recirculated until a time-dependent course of a dry matter concentration c (t) of the powdery substance P in the mixed product M has grown to the predetermined end value c E.
  • a formulation of the mixed product M is given, at least with regard to the time-dependent curve of a dry matter concentration c (t) assigned to the given end value c E , and the reaction conditions are given in the form of the default data D in each case.
  • the inventive solution concept corresponds in essential features to that according to the first method.
  • the multi-stage process in the second phase of the second method results in the time-dependent course of a dry matter concentration c (t), which ends as planned in the specified end value c E , with between the course of a dry matter concentration c (t) without saturation character ( approximately linear time-dependent course; see Figure 5 ) or with saturation character (degressive time-dependent course; see Figure 6 ) is to be distinguished.
  • the time-dependent course of a dry matter concentration c (t) ending in the predetermined end value c E is defined by the sequence of specific metering pulses i, ie clearly defined by the duration of the metering pulse ⁇ t1 and the time interval between adjacent metering pulses ⁇ t2.
  • the related course of a reference current consumption I o (t) is stored in the specification data D, and it is dependent on the recipe of the mixed product M and the reaction conditions for the mixing process.
  • the duration of the dosing pulse ⁇ t1 for the subsequent dosing pulse is shortened in the first case and lengthened in the second case.
  • the duration of the metering pulse ⁇ t1 is shortened according to the invention with a constant duration-time interval ratio V (as shown in FIG Figure 4 in contrast to Figure 3 is shown qualitatively as an example) or extended.
  • This technical control measure with a fixed time duration / time interval ratio V inevitably leads in the same ratio to a corresponding shortening or lengthening of the time interval between adjacent metering pulses ⁇ t2, based on the subsequent metering pulse i.
  • the mass flow of powdery substance ⁇ P is introduced into an existing almost unchangeable volume of the mixed product V M (V M ⁇ constant) in the time period t of the entire mixing process with an almost unchangeable fill level N in the mixing container 100, with a density ⁇ M of the mixed product M increasing, namely according to the time-dependent course of a dry matter concentration c (t), which grows to the predetermined end value c E.
  • a related course describes a successful mixing process, which on the one hand protects the mixed product M and on the other hand is designed to be energy-efficient. It does not require any control measures in the sense explained above. Only when deviations from the permissible current excess or current shortfall ⁇ I1, ⁇ I2 occur, do the control mechanisms, as used in the first method in connection with the Figures 3 and 4 have been described.
  • control measures with a variable duration-time interval ratio V require the control device 30 to be able to shorten or lengthen the duration of the metering pulse ⁇ t1 with an unchanging time interval between adjacent metering pulses ⁇ t2 or to adequately adjust the time interval between adjacent metering pulses ⁇ t2 with the same duration of the metering pulse ⁇ t1 lengthen or shorten.
  • control measures according to the invention therefore essentially consist in both embodiments of the second method in that the duration of the metering pulse ⁇ t1 and the time interval between adjacent metering pulses ⁇ t2 are selected in such a way that at the end of the time interval between adjacent metering pulses ⁇ t2 the time-dependent determined current consumption I (t) for stirring and / or mixing and homogenizing the temporarily present mixed product M * approximates the time-dependent course of a reference current consumption I o (t), which is required for the relevant treatment of the homogenized mixed product M, within the scope of a practically relevant permissible tolerance.

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Claims (14)

  1. Procédé de régulation de l'introduction d'une substance sous forme de poudre(P) dans un liquide (F) constitué d'au moins un composant pour un procédé de mélange en ligne,
    • lors duquel l'introduction et le traitement de la substance sous forme de poudre (P) se déroulent dans les conditions d'un comportement de distribution des temps de séjour d'une cuve de réaction homogène à fonctionnement continu, de telle sorte
    ∘ que le liquide (F) alimente en continu un mélangeur (100), sachant que l'objectif vise une concentration de matière sèche (c) prédéterminée temporellement invariable de la substance sous forme de poudre (P) dans le liquide (F),
    ∘ que le liquide (F) et la substance sous forme de poudre (P) sont remués constamment et/ou mélangés sous la forme d'un produit de brassage (M) et le produit de brassage (M) est homogénéisé et
    ∘ que le produit de brassage (M) est évacué en continu en fonction des quantités amenées de liquide (F) et de substance sous forme de poudre (P),
    • lors duquel une préparation du produit de brassage (M) au moins quant à la concentration de matière sèche (c) prédéterminée et les conditions de réaction sont respectivement prédéterminées sous la forme de données de consigne (D),
    caractérisé en ce
    • que la substance sous forme de poudre (P) alimente en discontinu le mélangeur (100),
    • que l'amenée discontinue de la substance sous forme de poudre (P) se déroule par impulsions moyennant une séquence temporelle d'impulsions de dosage (i), qui sont caractérisées respectivement par un débit massique de la substance sous forme de poudre (ṁP), par une durée de l'impulsion de dosage (Δt1) et par un intervalle de temps entre des impulsions de dosage proches (Δt2),
    • que la concentration de matière sèche (c) prédéterminée est définie par un rapport fixe durée-intervalle de temps V entre la durée de l'impulsion de dosage (Δt1) et l'intervalle de temps assigné entre des impulsions de dosage proches (Δt2) (V = Δt1/ Δt2 = constant),
    • qu'une consommation de courant (I(t)) est calculée en fonction du temps, qui est proportionnelle à une puissance d'agitation et/ou de cisaillement et d'homogénéisation nécessaire à un produit de brassage (M*) disponible temporairement,
    • qu'une consommation de courant de référence (Iο) est exploitée sur la base des données de consigne (D), qui est caractéristique de la puissance d'agitation et/ou de cisaillement et d'homogénéisation à fournir sur le produit de brassage (M) homogénéisé, et
    • qu'à la fin de l'intervalle de temps entre des impulsions de dosage proches (Δt2) et en cas d'écart de la consommation de courant (I(t)) en fonction du temps par rapport à la consommation de courant de référence (Iο), la durée de l'impulsion de dosage (Δt1) applicable à l'impulsion de dosage suivante (i) est raccourcie dans le premier cas et rallongée dans le second cas de plus d'une tolérance prédéterminée, et ce vers le haut ou vers le bas, tout en respectant le rapport fixe durée-intervalle de temps (V).
  2. Procédé de régulation de l'introduction d'une substance sous forme de poudre (P) dans un liquide (F) constitué d'au moins un composant pour un procédé de mélange en ligne,
    • lors duquel l'introduction et le traitement de la substance sous forme de poudre (P) se déroulent dans les conditions d'un comportement de distribution des temps de séjour d'une cuve de réaction homogène à fonctionnement continu, de telle sorte
    ∘ que du liquide (F) est collecté dans un mélangeur (100) et que la substance sous forme de poudre (P) est amenée en discontinu dans ce liquide (F) au cours d'une première phase,
    ∘ que le liquide (F) et la substance sous forme de poudre (P) sont remués constamment et/ou mélangés sous la forme d'un produit de brassage (M) et le produit de brassage (M) est homogénéisé,
    ∘ que le produit de brassage (M) obtenu au cours de la première phase est remis en circulation par le biais du mélangeur (100) et des quantités correspondantes de substance sous forme de poudre (P) sont encore amenées en discontinu dans la quantité recirculée de produit de brassage (M), et
    ∘ que le produit de brassage (M) recircule jusqu'à ce qu'une évolution en fonction du temps d'une concentration de matière sèche (c(t)) de la substance sous forme de poudre (P) dans le produit de brassage (M) parvienne à une valeur finale (cE) prédéterminée,
    • et lors duquel une préparation du produit de brassage (M) au moins quant à l'évolution en fonction du temps d'une concentration de matière sèche (c(t)) assignée à la valeur finale (cE) prédéterminée et les conditions de réaction sont respectivement prédéterminées sous la forme de données de consigne (D),
    caractérisé en ce
    • que l'amenée discontinue de la substance sous forme de poudre (P) se déroule par impulsions moyennant une séquence temporelle d'impulsions de dosage (i), qui sont caractérisées respectivement par un débit massique de la substance sous forme de poudre (ṁP), par une durée de l'impulsion de dosage (Δt1) et par un intervalle de temps entre des impulsions de dosage proches (Δt2),
    • que l'évolution en fonction du temps d'une concentration de matière sèche (c(t)) se terminant par la valeur finale (cE) prédéterminée est définie par la séquence d'impulsions de dosage (i) clairement fixées,
    • qu'une consommation de courant (I(t)) est calculée en fonction du temps, qui est proportionnelle à une puissance d'agitation et/ou de cisaillement et d'homogénéisation nécessaire à un produit de brassage (M*) disponible temporairement,
    • qu'une évolution en fonction du temps d'une consommation de courant de référence (Io(t)) est exploitée sur la base des données de consigne (D), qui est caractéristique de la puissance d'agitation et/ou de cisaillement et d'homogénéisation à fournir sur le produit de brassage (M) homogénéisé dans les conditions de l'évolution en fonction du temps assignée d'une concentration de matière sèche (c(t)), et
    • qu'à la fin de l'intervalle de temps entre des impulsions de dosage proches (Δt2) et en cas d'écart de plus d'une tolérance prédéterminée, et ce vers le haut ou vers le bas, de la consommation de courant (I(t) en fonction du temps par rapport à la valeur respectivement assignée de la consommation de courant de référence (Iο), la durée de l'impulsion de dosage (Δt1) applicable à l'impulsion de dosage suivante (i) est raccourcie dans le premier cas et rallongée dans le second cas.
  3. Procédé selon la revendication 2,
    caractérisé en ce
    que des évolutions en fonction du temps d'une concentration de matière sèche (c(t)) sans caractère de saturation sont définies par un rapport fixe durée-intervalle de temps (V) entre la durée de l'impulsion de dosage (Δt1) et l'intervalle de temps assigné entre des impulsions de dosage proches (Δt2) (V = Δt1/Δt2 = constant).
  4. Procédé selon la revendication 2,
    caractérisé en ce
    que des évolutions en fonction du temps d'une concentration de matière sèche (c(t)) avec un caractère de saturation sont définies par un rapport variable durée-intervalle de temps (V) entre la durée de l'impulsion de dosage (Δt1) et l'intervalle de temps assigné entre des impulsions de dosage proches (Δt2) (V = Δt1/ Δt2), sachant
    • qu'en cas d'écart de plus de la tolérance prédéterminée vers le haut de la consommation de courant (I(t)) en fonction du temps par rapport à la valeur respectivement assignée dans l'évolution en fonction du temps d'une consommation de courant de référence (Io(t)), le rapport durée-intervalle de temps (V) est diminué et
    • qu'en cas d'écart de plus de la tolérance prédéterminée vers le bas de la consommation de courant (I(t)) en fonction du temps par rapport à la valeur respectivement assignée dans l'évolution en fonction du temps d'une consommation de courant de référence (Io(t)), le rapport durée-intervalle de temps (V) est augmenté.
  5. Procédé selon l'une des revendications précédentes,
    caractérisé en ce
    que le débit massique de la substance sous forme de poudre (ṁP) est constant pendant la durée de l'impulsion de dosage (Δt1).
  6. Procédé selon l'une des revendications précédentes,
    caractérisé en ce
    que le raccourcissement ou l'allongement de la durée de l'impulsion de dosage (Δt1) se produit, dès lors qu'un corridor de courant fixé respectivement par un dépassement de courant vers le haut admissible (ΔI1) ou par un dépassement de courant vers le bas admissible (ΔI2) est quitté du fait d'une consommation de courant divergeant vers le haut (I*(t)) ou d'une consommation de courant divergeant vers le bas (I**(t)), sachant que le dépassement de courant vers le haut admissible et le dépassement de courant vers le bas admissible (ΔI1, ΔI2) sont fixés respectivement par une part en pourcentage de la consommation de courant de référence (Iο; Iο (t)) assignée.
  7. Procédé selon l'une des revendications précédentes,
    caractérisé en ce
    que le degré du raccourcissement ou de l'allongement de la durée de l'impulsion de dosage (Δt1) est fixé en fonction du degré de divergence de la consommation de courant en fonction du temps (I(t), I*(t), I**(t)) par rapport à la consommation de courant de référence (Iο; Iο (t)) assignée.
  8. Procédé selon l'une des revendications précédentes,
    caractérisé en ce
    que les autres données de consigne (D) dépendant de la préparation, sous-jacentes à la régulation de l'introduction de la substance sous forme de poudre (P) dans au moins un liquide (F) sont obtenues à partir des valeurs empiriques d'anciens procédés de mélange et enregistrées, dans lequel ces données de consigne (D) sont
    • un débit massique dudit au moins un liquide (ṁP),
    • une température de solution ou de mélange (T),
    • une pression au-dessus de la colonne de liquide (p),
    • les vitesses de rotation (n1, n2) d'installations d'agitation et/ou de mélange et d'homogénéisation et
    • un dépassement de courant vers le haut admissible (ΔI1) et un dépassement de courant vers le bas admissible (ΔI2) dépendant de la consommation de courant de référence (Iο; Iο (t)) assignée.
  9. Procédé selon l'une des revendications précédentes,
    caractérisé en ce
    que les paramètres de commande (S) opératoires dépendant de la préparation, obtenus au cours de la régulation de l'introduction de la substance sous forme de poudre (P) dans ledit au moins un liquide (F), à savoir
    • la durée de l'impulsion de dosage (Δt1) et
    • l'intervalle de temps entre des impulsions de dosage proches (Δt2) sont enregistrés et exploités en vue de réguler par la suite des préparations identiques.
  10. Procédé selon la revendication 2,
    caractérisé en ce
    que le produit de brassage (M) recirculé est divisé en une première fraction (a) et en une seconde fraction (b),
    que la première fraction (a) alimente directement le processus de mélange et que la seconde fraction (b) complémentaire passe par un volume de stockage et alimente ensuite pareillement le processus de mélange.
  11. Procédé selon la revendication 10,
    caractérisé en ce
    que la première fraction (a) se situe entre zéro et cent pour cent du produit de brassage (M) recirculé.
  12. Dispositif de mélange pour exécuter le procédé selon la revendication 1, avec un mélangeur (100), qui présente un raccord d'alimentation (100.5) servant à l'amenée d'un liquide (F), un raccord d'évacuation (100.4) servant à emmener un produit de brassage (M) et un agitateur (24) et/ou une installation de cisaillement et d'homogénéisation (26), avec une vanne d'admission (20) disposée sur le mélangeur (100) et dotée d'un organe de fermeture de vanne (8), avec l'organe de fermeture de vanne (8), qui permet de régler la vanne d'admission (20) entre complètement fermée (position de fermeture) ou complètement ouverte (position d'ouverture), avec la vanne d'admission (20), par laquelle une substance sous forme de poudre (P) est introduite dans le liquide (F), avec un système de commande (30) assigné à la vanne d'admission (20), avec lequel l'organe de fermeture de vanne (8) peut être mis dans la position de fermeture ou d'ouverture,
    caractérisé en ce
    • que le système de commande (30) fournit des données de consigne (D) dépendant de la préparation et des paramètres de commande (S) dépendant de la préparation sous la forme de la durée de l'impulsion de dosage (Δt1) et de l'intervalle de temps entre des impulsions de dosage proches (Δt2),
    • que le système de commande (30) présente au moins un capteur de signaux (16) conçu pour servir de système de mesure, qui détecte une consommation de courant (I(t)) en fonction du temps de l'agitateur (24) et/ou de l'installation de cisaillement et d'homogénéisation (26), et
    • que le système de commande (30) active la position de fermeture ou d'ouverture de l'organe de fermeture de vanne (8) en fonction de la consommation de courant (I(t)) dépendant du temps et en relation avec les données de consigne (D) et les paramètres de commande (S).
  13. Dispositif de mélange pour exécuter le procédé selon la revendication 2 avec les caractéristiques de la revendication 12,
    caractérisé en ce
    qu'une conduite de circulation (28) est prévue, qui bifurque d'une conduite reliée au raccord d'évacuation (100.4) et débouche directement dans le mélangeur (100).
  14. Dispositif de mélange selon la revendication 12 ou 13,
    caractérisé en ce
    que l'organe de fermeture de vanne (8) est conçu au moins dans sa zone soumise à la substance sous forme de poudre sous la forme d'une tige cylindrique d'un diamètre constant, sur laquelle un siège de vanne (8a) d'un même diamètre est façonné.
EP18718687.9A 2017-06-13 2018-04-03 Procédé et dispositif de mélange pour la régulation de l'introduction d'une substance sous forme de poudre dans un liquide pour un procédé de mélange en ligne Active EP3638411B1 (fr)

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DE102017005574.2A DE102017005574B3 (de) 2017-06-13 2017-06-13 Verfahren und Mischvorrichtung zur Steuerung der Einbringung eines pulverförmigen Stoffes in eine Flüssigkeit für ein Batch-Mischverfahren
PCT/EP2018/000148 WO2018228714A1 (fr) 2017-06-13 2018-04-03 Procédé et dispositif de mélange pour la régulation de l'introduction d'une substance sous forme de poudre dans un liquide pour un procédé de mélange en ligne

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WO2018228713A1 (fr) 2018-12-20
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DK3638411T3 (da) 2021-11-01
NZ759145A (en) 2020-11-27
EP3638409A1 (fr) 2020-04-22
EP3638411A1 (fr) 2020-04-22
JP6952802B2 (ja) 2021-10-20
EP3638409B1 (fr) 2021-08-04
AU2018285004A1 (en) 2019-12-12
NZ758627A (en) 2020-10-30
PL3638409T3 (pl) 2022-01-31
WO2018228714A1 (fr) 2018-12-20
AU2018285478A1 (en) 2019-11-21
PL3638411T3 (pl) 2022-01-31
AU2018285478B2 (en) 2020-12-10
AU2018285004B2 (en) 2020-11-12

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