• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    EMULSIFICATION DEVICE FOR CONTINUOUS PRODUCTION OF EMULSIONS AND / OR DISPERSIONS. The invention relates to an emulsification device for the continuous production of emulsions, nanoemulsions and / or dispersions with liquid-crystalline structure with a) at least one mixing device, b) at least one drive for the stirring member and c) at least one lifting device for each component or mixture of components.
    公开号:BR112012028569B1
    申请号:R112012028569-6
    申请日:2011-05-06
    公开日:2020-10-27
    发明作者:Gerd Dahms；Andreas Jung；Henrik Dörr
    申请人:Otc Gmbh；
    IPC主号:
    专利说明:

    [001] The present invention relates to an emulsifying DCE device for the continuous production of emulsions and / or dispersions. The emulsification device according to the invention can be used both for the production of classic, conventional biphasic emulsions, polyphasic emulsions, such as, for example, multiple emulsions and dispersions, as well as three-phase emulsions (OW), which, in addition to dispersed oily phase, still contain a liquid, crystalline gel network phase, but also for the production of liquid-crystalline pearlescent shine agents, liquid-crystalline self-organizing systems (gel network phases in OW emulsions), such as, for example, hair conditioners, as well as cleaning agents for skin and hair, such as shampoos, shower gels, wax and silicone emulsions and perfluorether emulsions, etc. The emulsification device can be used in the washing and cleaning agent industry, in the cosmetics industry, pharmacy, paint and varnish industry, but also in the food industry.
    [002] From the state of the art devices are known for producing emulsions and / or dispersions, which, in general, are used to carry out batch batch processes.
    [003] The document WO 2004/082817 describes a device for the continuous production of emulsions or dispersions under exclusion of air, which comprises a mixing device closed on all sides, which has supply and discharge tubes for entering and leaving materials or mixtures of fluid materials, as well as a stirring organ, which allows the introduction of stirring in the emulsion or dispersion, without generating cavitation forces and in high pressure homogenization.
    [004] EP 1 964 604 A2 describes a device and a process for the continuous production of a mixture of at least two fluid phases with a mixing vessel closed on all sides, rotatingly symmetrical or rotating symmetrically about its axis longitudinal, at least two feed lines leading to the mixing vessel, for the introduction of, in each case, a fluid phase of at least one discharge line, exiting the mixing vessel, for discharge of a mixed mixture of these phases and a rotary agitator, with paddle agitators for agitating the phases, whose axis of rotation is located on the longitudinal axis of the mixing vessel. With the device according to EP 1 964 604 A2, a controlled extensible current cannot be generated and measures are not taken to prevent turbulence and cavitation forces.
    [005] The task of the present invention is an emulsification device, with the help of which is possible the continuous production of emulsions, nanoemulsions and / or dispersions with liquid-crystalline structure.
    [006] According to the invention, the task is solved by an emulsifying device for the continuous production of emulsions and / or dispersions, with a) at least one mixing device, comprising - a rotationally symmetrical chamber, closed in all the air-tight sides - at least one supply line, for introducing fluid components, - at least one discharge line, for discharging the mixed fluid components, - a stirring element, which guarantees a laminar flow, with elements of agitation fixed on an agitator axis, whose axis of rotation extends along the axis of symmetry of the chamber and whose agitator axis is guided at least unilaterally,
    [007] being that at least one supply line is arranged in front of or below the at least one discharge line,
    [008] and the relation between the distance between the supply line and the discharge line and the diameter of the chamber is> 2: 1,
    [009] and the relationship between the distance between the supply line and the discharge line and the length of an agitation arm of the agitation elements is 3: 1 to 50: 1,
    [0010] and the ratio of the diameter of the agitator shaft to the inner diameter of the chamber makes up 0.25 to 0.75 times the diameter of the chamber,
    [0011] so that in the mixing device the components introduced through at least one supply line and mixed continuously through a turbulent mixing region on the supply side, in which the components are mixed in turbulent by the forces of shear exerted by the agitation organs,
    [0012] a percolation mixing region adjacent to it, in which the components are further mixed and the turbulent current decreases,
    [0013] a laminar mixing region on the discharge side, in which a lyotropic liquid-crystalline phase is formed in the mixture of the components,
    [0014] are transported in the direction of the discharge line, b) at least one drive for the stirring member and c) at least one transport device for each component or each mixture of components.
    [0015] The percolation mixing region is the transition region of the mixture, in which the same turbulent current passes to the laminar current, in which the percolation region adjacent to the turbulent mixture increases viscosity, caused by constant crushing of the droplets or by the formation of liquid crystalline phases and the turbulent current decreases. After reaching the critical Reynold index, the mixture moves to a mixed laminar region. In the mixed laminar region, then, under conditions of extensible current, the rupture of the drops is controlled and energy efficient, during the mixing process or the formation of liquid-crystalline phases.
    [0016] The chamber of at least one mixing device is symmetrically rotating and preferably has the shape of a hollow cylinder. However, the chamber may also have the shape of a truncated cone, a funnel, a truncated dome or a shape composed of these geometric shapes, with the diameter of the chamber from the supply line to the discharge line remaining the same or decreasing. The stirring member is adapted according to the shape of the symmetrical rotation chamber.
    [0017] The diameter of the agitator shaft dRw with respect to the inner diameter of the dK chamber is preferably within the range of 0.25- 0.75 * dK and the relationship between the distance between the supply line and the discharge and the length of the arms of the stirring elements is preferably within the range of 3: 1 - 50: 1, particularly preferably within the range of 5: 1 - 10: 1, especially within the range of 6 : 1 - 8: 1. The extraordinarily large diameter of the agitator shaft in relation to the chamber diameter also results in the fact that the distance between the agitator shaft and the chamber wall - also known by the technician as "creep diameter" - is always such small way that a chain cannot form like a thrombus and a laminar flow is guaranteed.
    [0018] The ratio of the distance between the supply line and the discharge line to the diameter of the chamber at the bottom of the at least one mixing device amounts to> 2: 1. In a divergent form of a hollow cylinder of the symmetrical rotation chamber, the distance between the supply line and discharge line for the chamber diameter in the region of the supply line of the at least one mixing device is also> 2: 1.
    [0019] The mixing device is closed on all sides and is operated without air exclusion. The components to be mixed are introduced as flowing streams into the mixing device chamber, mixed through the mixing organ, until the mixed components reach the discharge line and are discharged in such a way that no air enters the mixing device chamber. . The mixing device, in this case, is configured in such a way that there is as little dead space as possible. Upon entry into operation of the mixing device, within a short time, the air contained in it is completely displaced by the introduced components, with which the application of a vacuum is advantageously dispensed with.
    [0020] As the system works under exclusion of air and the components to be emulsified are continuously introduced into the mixing device, the components that are in the mixing device are transported continuously in the direction of the discharge line. The mixed components gradually pass through the mixing device, starting with the feed towards the discharge.
    [0021] In the mixing device according to the invention, the components fed through the feed lines, after entering the chamber, pass through a turbulent mixing region, in which they are first mixed turbulently by the shear forces exerted by the organs stirring. In that case, the viscosity of the mixing product is already noticeably increased. Further in the direction of the discharge line, the mixture then passes through a so-called percolation region, in which, due to another intensive mixture, the viscosity of the mixture additionally increases and the system gradually changes into a self-organizing system. Turbulences in the predominant current in the mixture gradually decrease when reaching the percolation region and the current conditions become increasingly laminar towards the discharge lines. In this way, a liquid-crystalline, lyotropic phase is formed in the mixture towards the discharge line.
    [0022] Advantageously, the total energy consumption of the emulsification device according to the invention is extremely low. This low total energy consumption results from the fact that in mixing devices, compared to conventional mixing processes, only small volumes need to be mixed and temperature-controlled. Therefore, high cost and high energy consumption heating and cooling processes are minimized and contribute decisively to low total energy consumption. The residence time of the mixing material in the mixing chamber is also very short. At a production capacity of 1,000 kg / h, the residence time averages between 0.5 and 10 seconds. It also follows that the supply lines and pumps are also substantially smaller in size and therefore the pump drives also absorb substantially less energy.
    [0023] Advantageously, the favorable relationship between the distance between the supply and discharge line and the length of the arms of the stirring elements, which is advantageously within the scope of 3: 1 -50: 1, particularly preferably, 5: 1-101, especially within the scope of 6: 1-8: 1, in connection with the special wire stirrers, contributes to guaranteeing a particularly efficient use of torque and, therefore, a good mixture is obtained, a, simultaneously, minimized engine power consumption.
    [0024] In addition, the exceptionally large shaft diameter in relation to the chamber diameter, allows the agitator shaft itself to be used for product temperature regulation, which, in turn, contributes to the total energy consumption under the emulsification device according to the invention.
    [0025] Due to the favorable ratio of the diameter of the chamber to its height and the agitation device optimized for the maintenance of a laminar flow, the power take-off of the motor of the agitation mechanism is substantially smaller and contributes decisively to the low total energy intake of the device according to the invention. By the components, which in this way can be dimensioned, in total, in a smaller way, a compact and space-saving construction method is characteristic for the mixing device according to the invention.
    [0026] The use of magnetic couplings also contributes to the reduction of total energy consumption. As the transmission of force from the motor to the motor shaft is made by permanent magnets, the motor only needs to produce the energy that is necessary for the rotation of the external rotor. The internal rotor, with a fixed agitator shaft, is moved by the magnetic force. Another advantage in connection with a slide bearing is that an airtight mixing chamber can be constructed.
    [0027] For optimum emulsification results and to avoid dead spaces, chambers are used in the mixing devices according to the invention, which have a symmetrical shape in rotation. These rotating symmetrical shapes are preferably hollow cylinders (figure 2a), but also a truncated cone (figure 2B), funnels (figure 2D), truncated dome (figure 2F) or shapes composed of them (figure 2C, E), in which, for example, a truncated cone-shaped region is adjacent to a hollow cylinder-shaped region. The diameter of the mixing device remains constant, in this case, from the end on the supply side to the end on the discharge side (figure 2a) or it decreases (figure 2B-F);
    [0028] Particularly preferably, in the mixing device according to the invention, a chamber in the form of a hollow cylinder or a truncated cone is used, or with a shape composed of a region in the form of a hollow cylinder and a region in truncated cone shape. The cone trunc is advantageously distinguished by the fact that the diameter at the end of the feed side to the diameter at the end of the discharge side constantly decreases, while the diameter of the hollow cylinder remains constant in relation to the axis of rotation.
    [0029] Advantageously, the mixing device chamber and / or the supply and discharge lines can be adjusted in temperature together or individually.
    [0030] The components are fed to the mixing device via at least one supply line, which in diameter is adapted to the respective component and its viscosity and guarantees complete filling with the respective phase. Preferably, the mixing device according to the invention has at least two supply lines. In the event that a pre-mixing needs to be conducted to the mixing device, then the mixing device can also have only one supply line. The components to be emulsified or to be dispersed can also be introduced, before entering the mixing device, for example, through a Y-shaped connection, in a common supply line, before they arrive at the mixing device. mixture. In a common line, one can optionally find static pre-mixers or passive mixing devices, known to the technician. Component in the sense of the invention can be a pure substance, but also a mixture of several substances.
    [0031] The angle of entry of the nodis mixing power lines can be, in this case, within the range of 0 ° to 180 ° with respect to the axis of rotation of the mixing device. The feed lines can reach the chamber laterally from the side surface or from below, from the bottom surface.
    [0032] The supply and discharge lines can be connected with the camera at any time and in any extension of the lateral area. In order to guarantee an optimum mixture and, at the same time, a maximum residence time of the fed components, as well as to avoid dead spaces, the height of the feed line (s) is preferably located in the lower third. preferably in the lower quarter of the chamber, in relation to the height of the chamber. The outlet height of the discharge line is preferably in the upper third, preferably in the upper quarter, of the chamber, in relation to the height of the chamber.
    [0033] The diameter of the discharge line is dimensioned in such a way that the pressure formation, with respect to the high viscosity in the at least one or first mixing device, is minimized, but at the same time it is guaranteed that the discharge lines, at any time, they are completely filled with the mixture.
    [0034] Some products, such as, for example, three-phase OW emulsions, pearlescent gloss agents, as well as lyotropic liquid-crystalline phases of self-organizing systems, may require an additional time-shifted addition of components in the region of percolation of the first mixing device, which is above the height of the entry lines and below the height of the exit lines. For this reason, additional entry lines can be found in that region.
    [0035] The mixing device can be oriented in any way, so that the axis of rotation of the stirring member can assume any desired position, from horizontal to vertical. But, preferably, the mixing device is not arranged in such a way that the axis of symmetry of the chamber is vertically arranged, in which case the supply lines are mounted above the discharge lines. Particularly preferably, the mixing device is arranged in such a way that the axis of symmetry of the chamber is arranged vertically, in which case the supply lines are mounted below the discharge lines. In this case, the drive motor drives the stirring member, preferably from above, but, likewise, a drive from below is also possible.
    [0036] Surprisingly, it was found that in the geometry of the mixing device, the diameter of the agitator shaft dRw, with respect to the inner diameter of the dK chamber and the relationship between the distance between the supply line and the discharge line and the length of the arms of the stirring elements is decisive to ensure an optimal mixing of the fed phases. In this case, it was found that the ratio of the diameter of the dRw agitator shaft to the internal diameter of the dK chamber is preferably within the 0.25 - 0.75 * dK, particularly preferably within the range of 0.3 - 0.7 * dK, especially within the range of 0.4 - 0.6 * dK and the relationship between the distance between feed line and discharge line and the length of the arms of the stirring elements is preferably within the range of 3: 1 - 50: 1, particularly preferably within the range of 5: 1 - 10: 1, especially in the 6: 1 - 8: 1 range.
    [0037] This exceptionally large diameter of the agitator shaft in relation to the chamber diameter also has the consequence that the distance between the agitator shaft and the chamber wall - also designated by the technician also known as "creep diameter - it is always so small that a thrombus-like current cannot form and laminar flow is guaranteed.
    [0038] In addition, it was found that in the geometry of the mixing device, the relationship between the diameter of the mixing device chamber and the path, that the components to be mixed must travel from the feed to the discharge, is decisive to guarantee an optimal mixture of the fed phases. In this case, it was found that the diameter ratio for the distance between supply and discharge is preferably in the range of 1:50 to 1: 2, preferably 1:30 to 1: 3, especially in the range from 1:15 to 1: 5. The diameter of the chamber in the sense of the invention is the diameter at the bottom of the chamber.
    [0039] The ratio of diameter to supply and discharge distance plays a decisive role in controlling the current within the mixing device. Because, only when the initially turbulent current, which is present in the lower region of the mixing device, therefore, in the region of the component supply, the mixture reaches the laminar phase, through the so-called percolation region, the success of the emulsification is guaranteed. In this case, the exact delimitation of the individual regions is not possible, since the transition between the respective regions is smooth.
    [0040] As the amount of time required to form the lyotropic liquid-crystalline phase is different, depending on the components, the length of the mixing device can be adapted according to the product. The formation of self-organizing systems is influenced by the following factors: temperature within the system, water content, composition of the mixture, current profile, amount of shear and residence time.
    [0041] The mixing devices used in the emulsifying device and installation according to the invention are equipped with stirring organs, which guarantee a laminar flow, which guarantees the droplet division under laminar elongation conditions. According to an advantageous configuration of the invention, at least one component of the stirring element is arranged spaced apart and parallel to the inner wall of the chamber.
    [0042] Preferred stirring organs are whole or partial paddle or whole or partial wire shakers or a combination thereof.
    [0043] The droplet division under laminar elongation conditions advantageously leads to an extremely narrow particle size distribution around an average droplet diameter in the emulsion produced. Very often, the graph of the particle size distribution shows a shape very similar to a Gaussian curve. The particle sizes, which can be obtained with the device according to the invention, are in the range of 50 to 20,000 nm, depending on the composition of the emulsion and / or dispersion.
    [0044] The diameter of the dR stirring member, relative to the inner diameter of the dK chamber, is preferably in the range of 0.99 to 0.6 * dK. But the stirring organ is at least 0.5 mm away from the chamber wall. Preferably, the diameter of the stirring member is 0.6 to 0.7 * dK, particularly preferably 0.99 to 0.8 * dK.
    [0045] The diameter of the dRw agitator shaft, with respect to the inner diameter of the dK chamber, is preferably within the range of o, 25- 0.75 * dK, especially preferably within the range of 0.3 - 0.7 * dK, especially within the range of 0.4 -0.6 * dK.
    [0046] This exceptionally large diameter of the agitator shaft in relation to the chamber diameter also results in the fact that the distance between the agitator shaft and the chamber wall - also known by the technician as "creep diameter - is always so small that a thrombus-like current cannot form and laminar flow is guaranteed.
    [0047] The wire stirrers, which can be used in the device according to the invention, are distinguished by the fact that wires are mounted on the stirrer shaft. It was found, surprisingly, that good mixing results and minimal energy intake are obtained with them, when they are bent in the manner of a horseshoe or a rectangle with rounded corners and are connected with their ends with the axis of shaker.
    [0048] Also the arrangement on the axis can be different according to the product to be mixed. One or more wires bent in the shape of a horseshoe or rectangular can be arranged on the agitator shaft. In that case, a whole wire shaker or a partial wire shaker can be used.
    [0049] The whole wire stirrer (figure 3C) is characterized by the fact that it consists of at least two wires bent in the shape of a horseshoe or in the form of a rounded rectangle, which, with respect to the axis, are mounted opposite each other another on the axis and connected with it in the upper and lower region of the axis. The wires are in this case preferably positioned perpendicular to the central axis and / or are turned and / or rotated at an angle from 0 ° to 90 °, preferably from 0 ° to 45 °, particularly preferably from 0 ° to 25 °, to the left or to the right, with respect to the axis of rotation. The upper and lower length of the wires can be of the same or different lengths. Any number of wires can be arranged on the axis perimeter. In the empty space formed between the axis and the wire, other wires or any geometric shapes can be found.
    [0050] A wire diameter is preferred, which lies at most within the scope of the shaft diameter and at least is not less than 0.2 mm, a wire diameter of at most 15 is particularly preferred % of the shaft diameter and at least 0.5 mm, especially the scope of 10% of the shaft diameter and at least 1% of the shaft diameter.
    [0051] The partial wire stirrer (figure 3 D) is characterized by the fact that it consists of at least two wires bent in the shape of a U or horseshoe whose ends are connected with the shaft at any height. The wires are in this case preferably positioned perpendicular to the central axis and / or are turned and / or rotated at an angle from 0 ° to 90 °, preferably from 0 ° to 45 °, particularly preferably from 0 ° to 25 °, to the left or to the right, with respect to the axis of rotation. The upper and lower length of the wires, extended radially from the agitator shaft, can have the same or different lengths. Any number of wires can be arranged on the axis perimeter. In the empty space formed between the axis and the wire, other wires or any geometric shapes can be found.
    [0052] A wire diameter is preferred, which is at most within the scope of the shaft diameter and at least not less than 0.2 mm, a wire diameter of at most 15% is particularly preferred of the shaft diameter and at least 0.5 mm, especially the scope of 10% of the shaft diameter and at least 1% of the shaft diameter.
    [0053] Due to the favorable ratio of the diameter of the chamber to the diameter of the agitator shaft, in association with the advantageous wire agitators, a particularly efficient use of torque is guaranteed, which minimizes the force that the agitator organ exerts on the components to be used. be mixed, so that a good mixture is obtained, while at the same time minimized energy consumption of the engine.
    [0054] In addition, the exceptionally large shaft diameter, in relation to the chamber diameter, allows the agitator shaft itself to be used for product temperature regulation.
    [0055] In addition, whole blade and partial blade agitators have been particularly suitable.
    [0056] The whole paddle stirrer (figure 3 A) is characterized by the fact that it consists of at least two square, rectangular, horseshoe-shaped or trapezoid-shaped plates, with the corners of the plates being rounded, for prevent the formation of turbulent currents, with one side connected to the axis and the plates continuously extend from the upper region of the axis to the lower region of the axis. The plates are, in this case, preferably positioned perpendicular to the central axis and / or are turned and / or rotated at an angle from 0 ° to 90 °, preferably from 0 ° to 45 °, particularly preferably from 0 ° to 25 °, to the left or to the right, with respect to the axis of rotation. The upper and lower edges of the plates may have the same or different lengths. Any number of plates can be arranged on the axis perimeter. The individual blades can be provided with other geometric openings, such as holes or stamping.
    [0057] The partial paddle stirrer (figure 3 B) is characterized by the fact that it consists of at least two square, rectangular, horseshoe-shaped or trapezoid-shaped plates, one side being connected with the shaft in any time. The plates are, in this case, preferably positioned perpendicular to the central axis and / or are turned and / or rotated at an angle from 0 ° to 90 °, preferably from 0 ° to 45 °, particularly preferably from 0 ° to 25 °, to the left or to the right, with respect to the axis of rotation. The upper and lower edges of the plates may have the same or different lengths. Any number of plates can be arranged on the axis perimeter. The individual blades can be provided with other geometric openings.
    [0058] Other stirring organs known to the technician and their special construction forms can be installed for mixing the product in the mixing device, such as, for example, the construction forms in anchor shaker, dissolver disk, itner-MIG etc. It is also possible to combine various forms of agitator construction on an agitator shaft.
    [0059] The stirring organs used in the mixing device according to the invention are further distinguished by the fact that each agitator axis is guided in a stable manner in rotation, for this purpose, preferably in the upper and lower regions. bottom of the mixing device. In this way, imbalances of the agitation organ at high rotation numbers must be excluded or substantially avoided, so that turbulence cannot be generated, which influence or even prevent the formation of the necessary laminar current. For conducting the shaft, for example, ball bearings, linear ball bearings, plain bearings, linear plain bearings or the like. For additional rotation stability, the shaft is advantageously balanced.
    [0060] The materials from which both the mixing device itself and the forms of construction of the agitators described above are produced, particularly the whole blade agitators, partial blade agitators, whole wire agitators and partial wire agitators, mentioned above, they are adapted to the chemical properties of the components to be emulsified and to the emulsions formed. Preferably, the stirring members in the mixing device according to the invention comprise, for example, fine steels, but also construction steels, plastics, such as, for example, PEEK, PTFE, PVC or plexiglass or composite materials or combines - steel and plastic sections.
    [0061] The mixing devices are designed in such a way that by themselves they only oppose a small back pressure to the components to be emulsified. For this reason, the mixing device can be designated as a substantially pressure-free / reduced pressure system.
    [0062] To achieve this, the cross section of the discharge line needs to be selected in such a way that the total product quantity of the mixed components can flow without hindrance. In this case, exactly the increase in extreme viscosity in the mixing device 1 must be observed, which results in the formation of the highly viscous liquid-crystalline gel-crystalline phase. Also when dimensioning other process components, such as, for example, pipes, heat exchangers, etc., it should be noted that they only oppose minimum pressure drops to the total system, to ensure a continuous system of reduced pressure. Depending on the product and configuration of the devices, pressure drops of below (0.5 bar) can be carried out in the total system.
    [0063] In the emulsification device according to the invention, temperature regulation of the mixing device, as well as of the supply and discharge lines, can be carried out in a particularly simple and efficient way. Due to the small volumes and the large ratio, determined by the shape of the chamber, from surface to volume of the chamber in the mixing device, in the device according to the invention a better controlled temperature conduction can be guaranteed compared to conventional emulsification devices .
    [0064] For heating the mixing devices, a double jacket is particularly suitable. It can be heated with gases, such as, for example, steam, or with liquids, such as, for example, water or thermal oil. Other possibilities are, for example, electric heaters, such as heating wires, heating cables or heating cartridges.
    [0065] For regulation of the components to be emulsified, inside and out, the mixing device is preferably equipped with a double jacket, cooling coils of whole or partial tubes, which are mounted on the outside and / or by inside the mixing device and are supplied with a cooling-heating medium, for example, through a thermostat.
    [0066] Preferably, the temperature conduction is improved by additional guide plates inside the double jacket. By optimizing the ratio of diameter to distance between supply and discharge lines, it is additionally possible to adapt the passage of the mixing product in such a way that an optimal temperature change is given.
    [0067] The device according to the invention, contrary to conventional batch processes, is distinguished by the fact that not all components of the recipe need to be heated, but that only those components that are not sufficiently fluid at room temperature are heated, until they are fluid. The configuration according to the invention of the mixing devices, particularly the length-diameter ratio, is so advantageous for the conduction of heat that the energy dissipated by the stirring can be used for controlled heat supply.
    [0068] In another embodiment, the mixing device according to the invention is equipped with current switches, which favor a laminar flow of the components.
    [0069] According to an advantageous configuration, the current switches and / or the stirring element can be regulated in temperature and, thus, allow a temperature regulation of the mixture.
    [0070] Preferably, the at least one mixing device comprises a symmetrical rotation chamber, in which the components to be emulsified, through the passage through a turbulent region and a percolation region, are transformed into a lyotropic liquid-crystalline phase.
    [0071] In another embodiment of the invention, the at least one mixing device comprises several symmetrical layers in rotation, connected one behind the other. With this it is possible that, for reasons of construction technique, the height of the at least one device mixing is limited, the mixing process can be divided into several successive chambers. In this case, the components pass through the three regions, turbulence region, percolation region and laminar region, not within a single chamber, but within several chambers.
    [0072] In the simplest case, the emulsification device comprises at least one mixing device according to the description above.
    [0073] Normally, however, the emulsification device according to the invention comprises at least two mixing devices, which are connected in series, one behind the other, and in which several components are fed successively or simultaneously and mixed together. . In that case, the viscosity of the mixture produced in the first mixing device is always greater than or equal to the viscosity in the subsequent mixing device (s). At least the first mixing device must correspond in structure and function to at least one mixing device, that is, in the first mixing device the special current conduction must be guaranteed, in which the components are first mixed in a turbulent way, then, through the passage through a percolation region, they reach a lyotropic liquid-crystalline state.
    [0074] In the production of classic two-phase systems, such as WO emulsions, but also OW emulsions, without gel mesh phase, in the emulsification device according to the invention the internal (dispersed) phase and (continuous) phase ratio in the first mixing device is always greater than in the subsequent mixing device (s).
    [0075] In the emulsification device according to the invention, it is also possible that several mixing devices are not only connected in series one after the other, but can also be connected in series one over the other or under the other In this case, the individual mixing devices can also be installed together in a housing, so that the separation of the mixing devices is not visible from the outside.
    [0076] And in the further course of producing the products cited in the emulsification device according to the invention, the highly viscous content of the first mixing device is guided to the subsequent mixing device (s). In that case, the supply to the subsequent mixing devices is configured in such a way that the height of the inlet lines is preferably in the lower third, preferably in the lower quarter, with respect to the height of the mixing device.
    [0077] In mixing devices connected downstream of the first mixing device, it is no longer necessary that the internal phase predominates over the continuous phase. In an embodiment of the emulsification device according to the invention, in the first mixing device the components to be emulsified are transformed into a laminar liquid-crystalline phase and in a second mixing device they are diluted to the desired concentration by adding an external phase .
    [0078] The emulsification device according to the invention also comprises corresponding peripherals, such as
    [0079] reservoirs for at least 2 components,
    [0080] connection lines for supplying components to the corresponding pumps and valves of at least one mixing device,
    [0081] connection lines for the discharge of components,
    [0082] control device for monitoring and regulating process stages,
    [0083] an indicating device with a maneuvering part for visualizing and entering process variables,
    [0084] the mixing devices and the connection lines can have the temperature regulated,
    [0085] mixing device and connection lines can have sensors for product and process control.
    [0086] In addition, the discharge lines of the individual mixing devices may have other sensors, which make it possible to measure the particle sizes continuously, directly or by bypass, a temperature measurement, a pressure measurement, a measurement conductivity, a viscosity measurement or the like.
    [0087] The product quality of the final product in the device according to the invention is determined, predominantly, in the first stirring stage.
    [0088] In addition, in the supply and discharge line of the mixing devices or in various mixing devices, between the mixing devices of an installation according to the invention, a heat exchanger can be fitted. It has been shown that the introduction of tube bundle heat exchangers in connection with helical guide plates in the product chain and guide plates in the heating and cooling circulation is very efficient. Due to the relatively small quantities of product, a very compact and efficient construction method for heat exchangers is advantageously possible. These heat exchangers can be used both in the series construction mode and in the queue-connected construction mode. The introduction of other forms of construction of heat exchangers, such as, for example, cooling coils, tube bundle heat exchangers, double tube heat exchanger, ribbed tube heat exchanger, spiral ribbon heat exchanger , plate heat exchanger, accumulator heat exchanger, and other special forms of construction are also possible.
    [0089] As refrigeration media, both gases, such as, for example, nitrogen, as well as liquids, such as, for example, water or thermal oil, can be used.
    [0090] With the heat exchangers mentioned above, both cooling and heating can be done. Here too, an appropriate heating / cooling for the desired product can be selected by the technician.
    [0091] Depending on the use of the emulsification device, optionally a combination of heating and cooling units is also possible. This, too, can be solved simply and efficiently, as described above, by using a double jacket, a heating / cooling coil or a corresponding heat exchanger.
    [0092] In smaller emulsifying devices, heating / cooling baths (thermostats) are particularly suitable for this purpose, which are preferably monitored and operated by a main control. Additionally, with these thermostats, stand-alone operation can also be made possible. As thermostats also generally have the possibility of connecting an external temperature sensor, it can be inserted into the product stream. The thermostat then regulates the required heating or cooling power automatically and thereby ensures an optimal product temperature. Another advantage of this method is a control discharge, since it can transfer the temperature regulation of the mixing devices to the thermostat.
    [0093] By optimizing the temperature of the component feed to the mixing devices, an optimization of the product temperature can also be obtained. In this way, the flow path of the components from the reservoir to the entrance to the mixing device can also be optimized and used to such an extent that the component streams reach the mixing device with an optimum temperature for the components to be emulsified.
    [0094] An emulsification device according to the invention comprises - at least one mixing device according to the invention, - at least one motor for the mixing devices of the mixing device, - at least two reservoirs for the phases to be emulsified, which are connected with the mixing device through the supply lines and from which the components are guided by means of transport devices, free of air, to the mixing device, - at least one device of transport for each component or for each mixture of components - optionally, input current monitoring sensors and / or output monitoring sensors, with which, optionally, an automatic quality control can be carried out simultaneously , - optionally, at least one temperature regulation device for the emulsification device and the line system for feeding and discharging components, mixtures of component es, - a control device for monitoring and controlling the mixing devices, the supply and discharge of the components, the mixtures of components, - optionally, an indicating device, with an operating field for visualization and data entry.
    [0095] Normally, however, the emulsification device according to the invention comprises at least two mixing devices, which are connected one behind the other, and in which several components are mixed in succession with each other. In that case, the viscosity of the mixture produced in the first mixing device is always greater than or equal to the viscosity in the subsequent mixing device (s). At least the first mixing device must correspond in structure and function to at least one mixing device, that is, in the first mixing device the special current conduction must be guaranteed, in which the components are first mixed in a turbulent way, then, through the passage through a percolation region, they reach a lyotropic liquid-crystalline state.
    [0096] In the production of classic two-phase systems, such as WO emulsions, but also OW emulsions, without gel network phase, in the emulsification device according to the invention the internal (dispersed) phase and (continuous) relationship ) external in the first mixing device is always greater than in the subsequent mixing device (s).
    [0097] The entire installation according to the invention is controlled through a programmable control in memory. It monitors, for example, the rotation numbers of the mixing devices, the inflow of the individual components, the rotation numbers of the pumps, the temperatures and pressures of the individual phases added and all the other parameters necessary for the operation. In connection with mass or volume flow meters, it can monitor and regulate the inflow of individual components in the respective mixing devices. It can relay previously defined warnings and defects through an optical or acoustic emission device. In this case, optical and acoustic emission can be separated from the device according to the invention, such as, for example, in a control center.
    [0098] Alternative control possibilities, such as, for example, software SPS or PC control are also possible, as well as a combination of several control possibilities.
    [0099] Through a remote maintenance module integrated with or connected to the control device, for connection of a telephone line or an ISDN line, access to a mobile radio network or a LAN network or WLAN, it is possible to carry out a remote maintenance of the device according to the invention or send communication of warnings and defects or control the entire installation according to the invention.
    [00100] In addition, the control may have a recipe module, in which one or more recipes for different products are deposited. In this case, each recipe can consist of several sets of data. In the data sets, the necessary parameters for the operation are recorded, such as, for example, the number of revolutions, the ratio of the volume current, etc. After consulting the recipe, the data sets are executed controlled in time, or after the start of a certain event, for example, when a certain temperature is reached. This makes it possible to guarantee that products of the same quality can always be produced.
    [00101] By means of the subsequent figures and examples of modality, the invention is explained in more detail, without limiting it. In this case, they show
    [00102] figure 1 an emulsification device with a mixing device,
    [00103] figure 2 various geometries of mixing devices
    [00104] figure 3 various agitating organs
    [00105] figure 4 emulsification device with a mixing device, with another supply line in the percolation region
    [00106] figure 5 emulsification device with two mixing devices
    [00107] figure 6 emulsification device with two mixing devices and heat exchanger
    [00108] figure 7 installation diagram
    [00109] figure 8 energy diagram
    [00110] Figure 1 shows in cross-section an emulsification device with a mixing device 1, with a symmetrical rotation chamber 2, closed on all sides, in the form of a hollow cylinder. In the chamber, an agitator shaft 10 is highlighted, on which agitation wires 11 are arranged, as shown in figure 3D. The agitator shaft 10 is driven by the motor 12 and guided by the bearings and seals 8. In addition, the agitator shaft 10 at the bottom of the chamber 2 is additionally guided by the bearing 9. The chamber 2 has supply lines at the bottom 5 or 6 for the air-free supply of components A and B and to be emulsified. In the upper part of the chamber 2, the discharge line 7 is arranged. The supply and discharge lines are also subject to temperature regulation and have corresponding lifting pumps (not shown in figure 1).
    [00111] The relationship between the distance between the supply lines 5 or 6 and the discharge line 7 and the diameter of the chamber 2 is approximately 3.5.
    [00112] The relationship between the distance between feed lines 5 or 6 and the discharge line 7 and the length of the stirring arms of the wire stirrers is approximately 15: 1.
    [00113] The chamber 1 is surrounded by the thermostat jacket 3, which in connection with the thermostat 4 allows a temperature regulation of the mixing material. Due to the greater distance in relation to the chamber diameter between supply and discharge, the mixing material can have its temperature regulated in a controlled manner, such that the introduction of energy caused by the agitator does not destabilize the mixing material.
    [00114] The emulsification device according to figure 1 can be used, for example, for the dilution of 100 kg per hour of sodium lauryl ether sulfate (SLES) as follows:
    [00115] Through the phase A pump, through the supply line 5, 41.4 kg per hour of 70% SLES are continuously guided and through the supply line 6, through the phase B pump, continuously, 58.6 kg per hour of water to the mixing device 1 and mixed with 3000 revolutions per minute.
    [00116] The mixing device 1 is closed on all sides and is operated without air exclusion. The components A and B to be mixed are introduced as fluid currents in the chamber 2 of the mixing device 1, mixed by means of the stirring organ 10 with the agitadro wires11, until the mixed components reach the discharge line 7 and, thus, are discharged in such a way that no air enters the chamber 2 of the mixing device 1.
    [00117] Upon entry into operation of the mixing device, the air contained in it is completely displaced, within a short time, by the components A and B introduced, with the advantage that the application of a vacuum is advantageously dispensed with.
    [00118] Mixed components A and B pass through chamber 2 of mixing device 1 gradually, starting from supply 5.6 to discharge 7. Components A and B introduced through supply lines 5, 6 in chamber 2 travel, initially, a turbulent mixing region on the feed side, in which they are turbulently mixed by the shear forces exerted by the stirrer wires 11. In a percolation mixing region that is adjacent above, the components are further mixed, being that the turbulent current decreases and the viscosity increases, until in a region of laminar mixing, on the discharge side, a lamellar liquid-crystalline, lyotropic phase is adjusted. Through the thermostat jacket 3, the temperature of the mixture is kept constant.
    [00119] 28% SLES is obtained at the exit of the stirring stage.
    [00120] Figure 4 shows in cross-section a one-stage emulsification device, which is formed and sized analogously to figure 1, but presents another supply line 13 for a component C. Supply and discharge lines are regulated in temperature and are interacting with pumps (not shown in figure 4).
    [00121] The emulsification device according to Fig. 4 can be used for the production of a simple O / W spray, as follows: Component A: aqueous emulsifier phase Component B: oily phase Component C: aqueous phase
    [00122] Component A is introduced at 8.1 kg per hour continuously through supply line 5 and component B, at 22.5 kg per hour, through supply line 6, free of air, in the chamber 2 of the mixing device 1 and mixed at approximately 3000 revolutions per minute. By means of the agitator 10 with the agitator wires 11, components A and B are mixed. After the mixture has traveled approximately 60% of the chamber length, component C is added through feed line 13 to the mixing chamber, at 69.4 kg per hour and mixed, until mixed components reach the discharge line. Upon entry into operation of the mixing device 1, the air contained in it is completely displaced, within a short time, by the introduced components, with which the application of a vacuum is advantageously dispensed with.
    [00123] The mixed components A and B travel through the mixing device 1 gradually, starting from the supply 5, 6 to the discharge 7. The components A and B introduced through the supply lines 5, 6 in the chamber 2, first pass through a region of turbulent mixing, on the feed side, due to the fact that they are mixed turbulently, by the shear forces exerted by the stirrer wires 11. In a percolation region that is adjacent above, components A and B are further mixed, being that the turbulent current decreases and the viscosity increases, until a liquid-crystalline, liotropic phase is established in a laminar mixing region on the discharge side, in which component C is fed through the supply line 13. Through of the thermostat jacket 3, the temperature of the mixture is kept constant.
    [00124] Figure 5 shows in cross-section an emulsification device with two mixing devices 1 and 1 '.
    [00125] The emulsification device according to figure 5 is distinguished by the fact that it consists of two mixing devices 1 and 1 connected in a row, the discharge line 7 of the first mixing device 1 being connected to the feed line of the subsequent 1 'mixing device. Mixing device layer 1 and 1 'has a thermostat jacket 3 or 3' and, when desired, can be individually regulated in temperature via thermostats 4 or 4 '. Shaking elements are wire stirrers attached to the stirrer shaft according to the representation of the 3D figure.
    [00126] The relationship between the distance between the supply lines 5 or 6 and the discharge line 7 and the diameter of the chamber 2 of the mixing device 1 amounts to approximately 2.0.
    [00127] The relationship between the distance between the feed lines 5 or 6 and the discharge line 7 and the length of the stirrer arms of the wire stirrers is 8: 1.
    [00128] The chamber 2 'of the mixing device 1 corresponds in structure and design to the chamber 2 of the mixing device 1.
    [00129] Mixing devices 1 or 1 'are equipped with sensors for viscosity, pressure, temperature (not shown here). Mixing devices 1 and 1 'are closed on all sides.
    [00130] The emulsification device according to figure 5 can be used for the production of a simple OW emulsion (120 kg per hour) as follows: Component A: emulsifier with additional base for neutralizing the thickening Component B : oily phase Component C: aqueous phase with thickener
    [00131] Component A is introduced at 5.65 kg per hour continuously, through supply line 5 and component B, at 21.93 kg per hour, through supply line 6 in chamber 2 of the device mix 1 and mixed with approximately 3000 revolutions per minute. By means of the stirring organ 10 with stirrer wires 11, components A and B are mixed until the mixed components reach the discharge line 7 and are diverted to the chamber 2 'of the mixing device 1', in such a way that no air enters chamber 2 of the mixing device 1. When the mixing device 1 and 1 'comes into operation, the air contained in it is completely displaced within a short time by the introduced components, with which it can be dispensed, advantageously, the application of a vacuum.
    [00132] The components A and B mixed pass through the mixing device 1 gradually, starting from the supply 5, 6 to the discharge 7. The components A and B introduced in the chamber 2 through the supply lines 5, 6, cross, first, a turbulent mixing region on the feed side, in which they are turbulently mixed by the shear forces exerted by the stirrer wires 11. In a percolation mixing region, which is adjacent above, components A and B are further mixed, the turbulent current decreases and the viscosity increases, until a laminar liquid-crystalline, lyotropic phase is established in a laminar mixing region on the discharge side. Through the thermostat jacket 3, the temperature of the mixture is kept constant.
    [00133] Phase C is introduced through feed line 13 in chamber 2 'at 72.42 kg per hour, together with the highly viscous mixture of components A and B. Through the agitator 10 and agitator wires 11 , the components are mixed until they reach the discharge line 7 'and are discharged in such a way that no air enters the chamber 2.
    [00134] In chamber 2 ', the highly viscous mixture of components A and B is diluted with the aqueous phase of component C to a fluent emulsion, with a particle size of 400 nm and a viscosity of 15,000 m Pas. In this case, the thickener serves to stabilize the emulsion and positively influences the sensation on the skin.
    [00135] Figure 6 shows in cross-section an emulsification device with two mixing devices 1 and 1 'and a plate heat exchanger 15. The emulsification device according to figure 6 is formed and sized analogously to the device emulsification system according to figure 5. The difference is the additional supply line 13 for component C, as well as the plate heat exchanger 15 in the discharge line 7 for supply to chamber 2.
    [00136] Mixing devices 1 and 1 'are equipped, in each case, with a thermostat jacket 3, which can be heated / cooled and connected in a row. Between the two mixing devices 1 and 1 'the product can be further heated and cooled by a plate heat exchanger.
    [00137] The emulsification device according to figure 6 can be used for the production of a pearly shine agent (100 kg per hour) as follows:


    [00138] Component A is introduced at 22 kg per hour and at room temperature, continuously, through supply line 5 and component B, at 24 kg per hour, at a temperature of 80 ° C, through the supply line 6 in chamber 2 of mixing device 1 and mixed at approximately 3000 revolutions per minute. The supply line 6 is temperature-controlled, so that component B is guided heated and with a temperature of 80 ° C to chamber 2.
    [00139] When components A and B mixed by means of the stirring organ 10 with the stirrer wires 11 reach the region of the feed line 13, component C is guided at 21 kg per hour and a temperature of 65 ° C at mixture. The thermostat jacket 3 of chamber 2 'is set in temperature to 65 ° C through the thermostat, so that components A, B and C are mixed at 65 ° C.
    [00140] After feeding component C, the mixture passes to a percolation region, until it reaches a liquid-crystalline, lyotropic state in the discharge line 7 region.
    [00141] Before the liquid-crystalline, lyotropic mixture, discharged through line and discharge 7, is fed to chamber 2 ', this mixture is cooled to 40 ° C through the plate heat exchanger 15 connected in line 7' . This is necessary, since the liquid-crystalline precursor, which is produced in the mixing device 1, is sensitive to temperature. Then, the liquid-crystalline precursor is diluted with phase D in the second mixing device 1 ', under countercooling by the heating / cooling jacket, at a temperature of 5 ° C. Product quality can only be obtained by observing this temperature profile . If the dilution with the cold D phase was made above 40 ° C, then product quality requirements could not be met. By cooling the product to too low a temperature, before dilution, a product is also obtained that does not satisfy the quality claims. This is due to the fact that the liquid-crystalline precursor assumes different liquid-crystalline structures, depending on the temperature, from which different final states are obtained in the dilution.
    [00142] Figure 7 shows a scheme of a complete emulsification installation for the production of a shampoo. The emulsification installation comprises 3 mixing devices 1, j1 'and 1 ", reservoirs A to D for components A to D to be mixed, connection lines for feeding components A to D to the corresponding mixing devices, with the corresponding E, E ', E ", E"' pumps, and valves, connection lines for the discharge of components, thermostats 4, 4 ', 4 "for temperature regulation of mixing devices 1, 1' and 1", a control device (not shown in figure 7), which monitors and regulates all process stages, an indicating device (not shown in figure 7), with a maneuvering part for visualization and introduction of process variables.
    [00143] The connection lines between the mixing devices 1 and 1 ', as well as 1' and 1 ", are equipped with temperature sensors to conduct the temperature of the mixing chambers. The mixing devices, as well as connection lines feature sensors for product and process control (not shown in figure 7). In addition, the discharge lines of the individual mixing devices may feature other sensors, which make it possible, for example, to measure continuous particle sizes directly or bypass (deviation), a temperature measurement, a pressure measurement or the like.
    [00144] By means of an example of emulsification for the production of a shampoo, the installation according to figure 7 is explained.
    [00145] The following components are stored in the reserve tanks: Component A: Sodium Lauret Sulfate (SLES) 70% Component B: water, preservative, co-active Component C: pearly shine agent Component D: water, salt, dyes
    [00146] The essential components form the three mixing devices 1, 1 ', 1 ", which are equipped, in each case, with a thermostat jacket and have their own heating / cooling circulation. In the mixing device 1 a highly viscous gel phase is generated from the individual components (component A, component B, component C). The mixing device 1 'serves to further agitate the gel phase, which is then guided to the mixing device 1 ", for there be diluted with component D.
    [00147] Component A, component B and component C are aspirated with pump, but with eccentric worm E, E 'and E "and fed to the first mixing device 1' in the ratio of 1: 3, 71: 0 , 36. Component D is fed to mixing device 1 "with pump E" 'in the ratio of 2.21 to component A. The pumps have been selected in such a way that they provide a uniform, non-pulsating component current In this case, each pump needs to provide a minimum, stable lifting chain, which is sufficient for a total production quantity of 100 kg up to 300 kg per hour. Eccentric worm pumps are very well suited in the diagram shown, once that they are not critical in relation to variations in viscosity.
    [00148] Due to the fact that in the installation shown schematically in figure 7 there are no flow meters for the individual product streams, it is advantageous to select a pump that has a characteristic line of linear elevation. In this way, alternating lift quantities can be calculated. In systems with flow meters (volume or mass), non-linear pumps, such as, for example, sprocket pumps, can also be used without problems.
    [00149] E pumps are designed for back pressure up to (5 bar). Using component A's sound, component D can simply be determined the amount of lift of the respective pump, at an adjusted number of revolutions. Here, the determination of the amount of lift in 100 U / min is presented. The corresponding lifting current is collected for the duration of one minute in a container, previously tared, and weighed. This process is repeated three times and from all three lifting currents the average value is formed. The average lifting current can then be calculated using the rule of three for the lifting current required for the recipe.
    [00150] With the speeds determined in this way, the pumps and motors of the agitation organs are now put into operation. The pumps now raise the required quantities of the individual components to the mixing devices to obtain the final product. Through the built-in pressure sensors P, the pressure formed can be controlled and, in the event of overpressure in the piping or in the mixing devices, the control can react accordingly and issue a warning to stop the installation or take similar countermeasures. Through the temperature sensor integrated in the discharge lines of the individual mixing devices, the temperature of the product can be detected and used to control the temperature regulation devices of the double jacket or be processed at another point in the control or in a peripheral device .
    [00151] In shampoo production, the total power of the complete installation was measured, depending on the total passage.
    [00152] Total power intake was measured at a production of 100 kg / h, 150 kg / h, 200 kg / h, 250 kg / h, 300 kg / h and 400 kg / h. The measured values determined were entered in an XY diagram (figure 8). Conditions: Emulsification installation with 3 mixing chambers Chamber diameter: 50mm Stirring tool: partial wire stirrer Measured values:

    [00153] When the values are extrapolated with the help of a statistical program, even at a production of 10,000 kg / h the energy requirement of 2 kW is not exceeded.
    权利要求:
    Claims (13)
    [0001]
    1. Emulsification device for the continuous production of emulsions and / or dispersions, comprising: (a) at least one mixing device (1), comprising: - a rotationally symmetrical chamber (2), closed on all sides to the air proof, - at least one supply line (5, 6), for introducing fluid components, - at least one discharge line (7), for discharging mixed fluid components, - a stirring member (11), which guarantees a laminar flow and comprises agitation elements fixed on an agitator axis (10), whose axis of rotation extends along the axis of symmetry of the chamber and whose agitator axis (10) is guided at least unilaterally, in that at least one supply line (5, 6) is arranged in front of or below the at least one discharge line (7), (b) at least one drive (12) for a stirring member, and ( c) at least one transport device per component or mixture of components, characterized by the fact that that the relationship between the distance between the supply (5, 6) and discharge (7) lines and the diameter of the chamber (2) is> 2: 1, with the relationship between the distance between the supply line (5) , 6) and discharge line (7) and the length of an agitation arm of the agitation elements is 3: 1 to 50: 1, and the ratio of the diameter of the agitator shaft (10) to the internal diameter of the chamber (2) is 0.25 to 0.75 times the diameter of the chamber (2), so that the components introduced into the mixing device (1) through at least one supply line (5, 6) can be mixed and transported continuously through a turbulent mixing region on the feed side, in which the components can be turbulently mixed by the shear forces exerted by the stirring organs (11), a percolation mixing region adjacent to it, in the which components can be further mixed and the turbulent current decreases, a mixing region l amine on the discharge side, in which a lyotropic liquid-crystalline phase can be established in the mixture of the components, in the direction of the discharge line (7).
    [0002]
    2. Device according to claim 1, characterized by the fact that the chamber (2) has the shape of a hollow cylinder, a truncated cone, a funnel, a truncated coupling or a shape composed of these geometric shapes , the chamber diameter remaining constant or decreasing from the feed line (5, 6) to the discharge line (7) and the stirring member (11) being adapted correspondingly to the chamber shape (2).
    [0003]
    3. Device according to claim 1, characterized by the fact that the relationship between the diameter of the chamber (2) and the distance between the supply line (5, 6) and the discharge line (7) is in the range of 1 : 50 to 1: 2.
    [0004]
    4. Device according to claim 1, characterized by the fact that the ratio of the diameter of the agitator shaft (10) to the inner diameter of the chamber (2) dK is preferably in the range of 0.3 - 0.7 * dK.
    [0005]
    5. Device according to claim 1, characterized by the fact that at least one component of the stirring elements is arranged in parallel and spaced from the inner wall of the chamber (2).
    [0006]
    6. Device according to claim 1, characterized by the fact that the stirring member (11) is a full-blade or partial-blade stirrer or a whole-wire stirrer or a partial-wire stirrer or a combination thereof .
    [0007]
    Device according to any one of claims 1 to 6, characterized in that the chamber (2) has at least one current switch (16) that favors a laminar flow.
    [0008]
    Device according to any one of claims 1 to 6, characterized in that the at least one mixing device (1) has several rotationally symmetrical chambers (2, 2 ') connected in series.
    [0009]
    9. Device according to claim 1, characterized in that the mixing device (1) as the first mixing device has at least one additional mixing device (1 ') connected downstream, a liquid-crystalline phase and lyotrophic being present in the mixture of the components downstream of the first mixing device (1), and the viscosity of the mixture in at least one additional mixing device (1 ') downstream being equal to or less than the viscosity downstream of the first mixing device (1).
    [0010]
    10. Device according to claim 1, characterized by the fact that at least one current sensor is arranged on at least one of the lines.
    [0011]
    11. Device according to claim 1, characterized by the fact that at least one temperature control device is coupled to at least one of the lines, so that the components, mixtures of components and / or emulsions or dispersions are cooled or heated.
    [0012]
    12. Device according to any one of claims 1 to 11, characterized in that the drive (12), the lifting device and the sensor, and the temperature control device are connected to a control device for monitoring and controlling the mixing devices (1, 1 '), the supply line and the discharge line of the components (5, 6, 7, 7', 13), mixtures of components, or emulsions or dispersions, the control device controlling the system in such a way that the viscosity of the mixture generated in the first mixing device (1) is always greater than or equal to the viscosity in the downstream mixing device (s) ( 1 ') and a laminar current of the mixed components is guaranteed.
    [0013]
    13. Device according to claim 12, characterized by the fact that the control device is connected or can be connected with a remote maintenance module and / or recipe management module.
    类似技术:
    公开号 | 公开日 | 专利标题
    BR112012028569B1|2020-10-27|emulsification device for continuous production of emulsions and / or dispersions
    BR112014030421B1|2021-04-06|AGITATOR FOR STABILIZING UNFINISHED LIQUID BINDING PRODUCTS INTENDED TO FORM CERAMIC ITEMS
    Prajapati et al.2009|CFD Investigation of the Mixing of Yield‐Pseudoplastic Fluids with Anchor Impellers
    BRPI0615949A2|2011-05-31|control system and method for material combination
    BRPI0907475B1|2019-04-24|VECTOR TYPE MIXER AND METHOD FOR OBSERVING A SUPERSATURATED FLUID SOLUTION OR FOLDER
    ES2691704T3|2018-11-28|Reaction chamber for a chemical reactor and chemical reactor constructed from this
    CN105664826B|2018-11-16|A kind of outer circulation type alkylation reactor and alkylation reaction method
    CN205627680U|2016-10-12|Continuous emulgator of mechanical stirring formula
    RU2572330C1|2016-01-10|Rector with multi-row mixers for treatment of fluid media
    CN207307862U|2018-05-04|Oiliness polyurethane synthesis system
    CN105642217B|2019-02-01|A kind of outer circulation type alkylation reactor and alkylation reaction method for strengthening conveying
    CN205627930U|2016-10-12|Extrinsic cycle formula alkylation reaction ware
    CN105664745B|2019-07-02|It is a kind of to strengthen the mechanical agitation type Continuous Emulsifier conveyed and emulsification method
    CN205850621U|2017-01-04|A kind of mechanical agitation type Continuous Emulsifier strengthening conveying
    CN205850826U|2017-01-04|A kind of outer circulation type alkylation reactor strengthening conveying
    CN109745899A|2019-05-14|The double high speed dispersion bottom homogenizer vacuum emulsification Manufacturing medicine extract machines of double oil cylinders
    CN206965598U|2018-02-06|Stirred tank
    CN209679985U|2019-11-26|The double high speed dispersion bottom homogenizer vacuum emulsification Manufacturing medicine extract machines of single cylinder
    KR20150010581A|2015-01-28|Agitating bar and agitator including the same
    CN208287838U|2018-12-28|A kind of efficient emulsion dispersion machine
    CN107456937A|2017-12-12|A kind of reactor
    CN213556401U|2021-06-29|Water-based resin circulation emulsification device
    CN106268433A|2017-01-04|A kind of chemical solution configuration equipment
    RU182466U1|2018-08-20|Device for mixing liquid media
    CN208260623U|2018-12-21|A kind of nano liposomes high-shearing vacuum homogeneous emulsifying machine
    同族专利:
    公开号 | 公开日
    US20130201785A1|2013-08-08|
    ES2528118T3|2015-02-04|
    PL2566609T3|2015-04-30|
    CN102946983B|2014-12-17|
    KR20130113935A|2013-10-16|
    BR112012028569A8|2020-01-07|
    EP2566609B1|2014-10-29|
    DK2566609T3|2015-01-26|
    CN102946983A|2013-02-27|
    CA2798705C|2017-03-14|
    CA2798705A1|2011-11-10|
    US10610835B2|2020-04-07|
    JP2013532047A|2013-08-15|
    WO2011138438A1|2011-11-10|
    KR101664402B1|2016-10-14|
    US9555380B2|2017-01-31|
    EP2566609A1|2013-03-13|
    BR112012028569A2|2016-08-02|
    JP5795794B2|2015-10-14|
    US20170120205A1|2017-05-04|
    DE102010028774A1|2011-11-10|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2667407A|1949-02-11|1954-01-26|Standard Oil Dev Co|Liquid-liquid contact method and apparatus|
    US3579461A|1967-11-20|1971-05-18|Johnson & Son Inc S C|Emulsification process|
    DE1757217A1|1968-04-11|1972-02-03|Petzholdt Maschf J S|Method and device for mixing, salifying and homogenizing pasty and flowable materials|
    US3807703A|1972-10-12|1974-04-30|Usm Corp|Mixer-emulsators|
    DE2357212A1|1973-11-16|1975-05-22|Henkel & Cie Gmbh|Water-in-oil emulsions for cosmetics continuously produced - by high speed mixing followed by shearing through narrow gap|
    DE2720683A1|1977-05-07|1978-11-09|Horst Groneweg Kg|Prepn. of emulsion, e.g. non-stick agent for use in baking - by feeding metered amounts of raw materials to tandem mixers with metered admixtures of water|
    US4123403A|1977-06-27|1978-10-31|The Dow Chemical Company|Continuous process for preparing aqueous polymer microsuspensions|
    US4155657A|1978-03-10|1979-05-22|Chemed Corporation|Continuous mixer for preparing emulsions|
    JPS57187626A|1981-05-13|1982-11-18|Omron Tateisi Electronics Co|Spectroscopic spectrum scanning device|
    JPS6034345Y2|1981-05-25|1985-10-14|
    JPH0336569B2|1983-05-06|1991-05-31|Fuji Photo Film Co Ltd|
    US5250576A|1991-08-12|1993-10-05|The Procter & Gamble Company|Process for preparing emulsions that are polymerizable to absorbent foam materials|
    US5149720A|1991-08-12|1992-09-22|The Procter & Gamble Company|Process for preparing emulsions that are polymerizable to absorbent foam materials|
    DE4202212A1|1992-01-28|1993-07-29|Basf Ag|CONTINUOUS METHOD FOR PRODUCING AQUEOUS POLYACRYLATE SECONDARY DISPERSIONS|
    JP3285427B2|1993-08-04|2002-05-27|冷化工業株式会社|Emulsion manufacturing apparatus and method|
    CN1095965A|1994-03-12|1994-12-07|青海大通机电厂|The emulsifying liquid method and apparatus|
    US5839827A|1996-03-28|1998-11-24|Kuraray Co., Ltd.|Agitating element for mixing apparatus and the mixing apparatus equipped with the agitating element|
    FR2747321B1|1996-04-16|1998-07-10|Centre Nat Rech Scient|PROCESS FOR THE PREPARATION OF AN EMULSION|
    DE19828742A1|1998-06-27|1999-12-30|Basf Coatings Ag|Taylor reactor comprising vertical rotor and wall in relative rotation, defining constant, divergent or convergent annular gap|
    US20030227817A1|2002-04-11|2003-12-11|Mobius Technologies, Inc., A California Corporation|Mixer|
    DE10242100A1|2002-09-11|2004-03-25|Hennecke Gmbh|Continuous mixing of polyol and isocyanate to produce reactive polyurethane mixture involves use of an impeller mixer with a specified number of angled blades in planes along the shaft|
    DE20321104U1|2003-03-21|2006-01-05|Ifac Gmbh & Co. Kg|Apparatus for the continuous production of emulsions or dispersions|
    CN2629819Y|2003-08-05|2004-08-04|温州市新特制药机械有限公司|Emulsion mixing device|
    WO2005039745A1|2003-10-16|2005-05-06|Basell Poliolefine Italia S.R.L.|Process for the continuous production of emulsions|
    EP1842576B1|2004-12-29|2011-11-16|Ultrasound Brewery|Method for ultrasonic separation of solution and ultrasonic separation apparatus for use in the method|
    DE102007005622A1|2007-01-31|2008-08-07|Hebold Mixing & More Gmbh|Liquid phases e.g. emulsions, mixture producing device, has discharge pipe arranged within region of passage of longitudinal axis through mixing vessel that is symmetrically rotated around its longitudinal axis|
    JP5246613B2|2007-12-27|2013-07-24|東洋紡株式会社|Vesicle using mannosyl erythritol lipid, emulsion composition and use thereof|
    JP5357660B2|2008-08-28|2013-12-04|花王株式会社|Method for producing water-in-oil emulsified cosmetic|DE102007063133A1|2007-12-24|2009-06-25|Sasol Germany Gmbh|Process for producing wax in water Dispersions from self-emulsifying gel concentrates|
    US9193105B1|2011-08-31|2015-11-24|Consolidated Nuclear Security, LLC|Casting fine grained, fully dense, strong inorganic materials|
    DE102012103885B4|2012-05-03|2015-07-23|Sonderhoff Engineering Gmbh|Apparatus for producing a multi-component mixture|
    WO2014196707A1|2013-06-03|2014-12-11| 엘지화학|Device for manufacturing polymer latex resin powder and method for manufacturing polymer latex resin powder using same|
    KR101594652B1|2013-06-03|2016-02-16|주식회사 엘지화학|Apparatus for preparing polymer latex resin powder and manufacturing method of polymer latex resin powder using the same|
    EP2823811A1|2013-07-09|2015-01-14|OTC GmbH|Targeted active release system comprising solid lipid nano-particles|
    CN104645857B|2013-11-25|2017-12-05|大连隆星新材料有限公司|Paraffin agitating device|
    DE102013018094A1|2013-12-03|2015-06-03|Merck Patent Gmbh|Mixing device and its use|
    JP2015175913A|2014-03-13|2015-10-05|三菱化学株式会社|Production method of toner for electrostatic charge image development|
    DE102015107027A1|2015-05-06|2016-11-10|List Holding Ag|Apparatus and method for carrying out mechanical, chemical and / or thermal processes|
    KR101574299B1|2015-05-21|2015-12-04|엔지니어스 주식회사|Manufacturing device of reinforcing ground material for improving surface layer|
    DE102015217551A1|2015-09-14|2017-03-16|Wacker Chemie Ag|Process for the continuous production of stable silicone emulsions|
    DE102016203293A1|2016-03-01|2017-09-07|Sandvik Materials Technology Deutschland Gmbh|Apparatus, plant and method for admixing at least a first substance and a second substance to a base material to form a mixture|
    EP3481932A1|2016-07-08|2019-05-15|Castrol Limited|Industrial fluid|
    JP2019520463A|2016-07-08|2019-07-18|カストロール リミテッド|Metalworking fluid|
    US20190225901A1|2016-07-08|2019-07-25|Castrol Limited|Industrial Fluid|
    JP2019520462A|2016-07-08|2019-07-18|カストロール リミテッド|Metalworking fluid|
    EP3481928A1|2016-07-08|2019-05-15|Castrol Limited|Industrial fluid|
    CN106074672B|2016-07-18|2021-10-29|四川科伦药业股份有限公司|Constant temperature system for improving quality of fat milk product|
    ES2684630B2|2017-03-30|2019-07-02|Inversiones Hiki6 S L|Method, software and multifunctional, modular and mobile mixing and packaging plant|
    EP3498253B1|2017-12-14|2021-02-17|Clariant International Ltd|Vesicles for delayed delivery of fragrance their preparation and use thereof|
    EP3508560A1|2018-01-05|2019-07-10|Castrol Limited|Micellar emulsions useful for metalworking applications|
    EP3508562A1|2018-01-05|2019-07-10|Castrol Limited|Micellar emulsions|
    EP3508552A1|2018-01-05|2019-07-10|Castrol Limited|Phase change material for heat exchange fluid/coolant|
    EP3508561A1|2018-01-05|2019-07-10|Castrol Limited|Micellar emulsions useful for metalworking applications|
    CN108904331A|2018-08-29|2018-11-30|她芙医美（厦门）科技有限公司|A kind of infant's camellia oil shampoo used also as bath lotion and preparation method thereof|
    EP3628304B1|2018-09-26|2021-07-14|Clariant International Ltd|Cosmetic gel comprising a triglyceride oil|
    EP3677244A3|2020-02-04|2020-11-18|Clariant International Ltd|Compositions comprising multilamellar vesicles|
    WO2021156213A1|2020-02-04|2021-08-12|Clariant International Ltd|Lipid nanoparticles for delayed delivery of fragrance with enhanced water solubility, their preparation and use|
    WO2021175583A1|2020-03-06|2021-09-10|Clariant International Ltd|Lipid nanoparticles comprising a fragrance|
    法律状态:
    2018-04-10| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2019-02-19| B06T| Formal requirements before examination [chapter 6.20 patent gazette]|
    2019-12-31| B06A| Patent application procedure suspended [chapter 6.1 patent gazette]|
    2020-06-02| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2020-10-27| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 06/05/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    2022-03-03| B21F| Lapse acc. art. 78, item iv - on non-payment of the annual fees in time|Free format text: REFERENTE A 11A ANUIDADE. |
    优先权:
    申请号 | 申请日 | 专利标题
    DE102010028774.1|2010-05-07|
    DE102010028774A|DE102010028774A1|2010-05-07|2010-05-07|Emulsifying device for the continuous production of emulsions and / or dispersions|
    PCT/EP2011/057315|WO2011138438A1|2010-05-07|2011-05-06|Emulsification device for continuously producing emulsions and/or dispersions|
    [返回顶部]