• 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:
    Processing unit for a flowing liquid, which extends around a virtual flow axis (S) which is also the longitudinal axis of the processing device and which is composed of: an inflow section (12), which for the inflow of the liquid into the installation is connected or connectable to a liquid line running around the axis of a line (at S), wherein the inflow section has an inflow opening (24) through which liquid can flow into the processing plant (10), - a, related to the flow axis ( S), flowable spiral section (14) connectable axially to the inflow section (12), the flowable space (28) of which runs spirally around the flow axis (S), an outflow opening (48) axially following the spiral section (14) the liquid flowing through the installation can freely flow out, characterized in that the inflow section (12) is constructed such that the flow axis (S) of the installation is coaxial with the axis of the liquid line is connected, or will be connectable, and that the surface flow through the liquid (32a, 34a, 36a) of the spiral-shaped flowable space (28) of the spiral section (14) decreases along the flow axis (S) in the direction from the inflow opening (24) to the outflow opening (48).
    公开号:NL1042036A
    申请号:NL1042036
    申请日:2016-09-06
    公开日:2017-03-17
    发明作者:Cornelis Magdalenus Benjamin Kamp Ir
    申请人:Cornelis Magdalenus Benjamin Kamp Ir；
    IPC主号:
    专利说明:

    Processing unit for flowing liquids Description
    The invention relates to an installation for processing a liquid flowing through it, which is built up around a virtual flow axis, which is the longitudinal axis of the installation, and which consists of: - An inflow section, which, around the liquid in the installation to flow in, is connected or can be connected to a liquid line, which runs around the axis of the line, wherein the inflow section has an inflow opening through which the liquid can be introduced into the installation. - A flowable spiral section which can be connected axially to the inflow section with respect to the flow axis, the flowable spiral section of which the flowable space runs spirally about the longitudinal axis of the installation. - An outflow section which connects axially to the spiral channel, whereby the liquid flowing through the installation leaves the installation as a free jet.
    A device for treating water as a liquid with all the features of the general main claim before us is known from a Chinese application with number 201310470765.7. This application has been made public under number CN 103539221 A.
    The purpose of this generic device is to whirl the water flowing through it to the maximum before allowing it to flow freely through the outflow opening with a maximum degree of swirl.
    In this case it is essential for such a generic device that the water flows into the inflow segment through two or more liquid lines placed orthogonally to the virtual flow axis. As a result of this method of introduction, the water initially flows with a high initial degree of swirling, rotating about the virtual flow axis, into the input segment and then flows from the input segment into the connected spiral section, the water apparently retaining the intake recorded at the inflow. impulse, flows into the spiral and to be further accelerated there.
    The purpose of the aforementioned generic device is an unspecified "activation" of the water flowing through it. The technical and scientific backgrounds of this device are not fully explained.
    Another device for processing water by means of a spiral section is known from DE 20 2008 009 583 U1. This document describes how one or more channels spiral around the cylinder axis over the surface of a cylindrical body. The cylindrical body can be mounted in a water pipe by means of an enveloping outer cylinder which is provided with suitable spiral grooves.
    This device would reduce the conductivity of the water flowing through, increase the purity and reduce the dissolved gas content. The operation of this device would, according to the description in the text, be based on a strong swirl of the water during the flow of the device. The working method of this device is also not explained scientifically.
    The object of the present invention is to introduce an installation with which the properties of liquids, in particular water, can be changed by mechanical and dynamic influence. In particular, it will be possible to increase the amount of gas dissolved in the water, in particular oxygen, and to improve the subjective experience of taste and freshness in consuming water processed in this way.
    This objective is achieved by a generic device, the inflow section of which is designed in such a way that the flow axis is connected or connectable to this conduit coaxially with the axis of the fluid conduit, the surface area of the cross-section of the space through which the fluid flows. formed by a spiral section, becomes smaller in the direction from inflow to the outflow opening.
    The proper functioning of the installation proposed here is first of all the axial flow of liquid up to the installation through an adequate orientation of the connection of the inlet opening of the installation to the supply line. This connection method avoids swirling of the liquid entering the installation.
    Rather, the liquid is guided only through a spiral channel connected to the inlet opening in a path around the virtual flow axis, the bend or rotation of this path becoming stronger as it progresses along the flow axis, because the radius of curvature with which the spiral fluid channel extends wraps about the longitudinal axis decreases in the direction from inlet opening to the outlet opening. The decrease in this radius of curvature, at a constant flow rate, effects an increasing centripetal acceleration acting on the fluid along the flow axis.
    The cross-sectional area of the spiral channel through which the fluid flows is also reduced in the direction from the inlet opening to the outlet opening, which leads to an increasing acceleration of the liquid in the flow direction with the generally not being compressible of liquids. .
    This leads at the outlet opening, that is, where the liquid flows out freely, not guided through pipes, to effects which achieve the above stated technical objective. Due to the increasing deflection around the flow axis as well as to increasing acceleration in the direction of the outflow opening, there is a strong atomization of liquid around the free-flowing liquid jet at the outflow opening. This leads, on the one hand, to an increase in the surface area of the outflowing liquid jet, and, on the other hand, as a result of the formation of droplets in the sub-micrometer domain, influences arise on the distribution of the electrical charge in the liquid flowing out of the installation.
    In particular, a difference in the distribution of charge that can be detected with measuring equipment is created, with charge carriers of the one polarity being mainly present in the spray mist around the outflow opening, while charge carriers of the opposite polarity mainly reside in the free-flowing liquid itself.
    The effect of the charge distribution, combined with an increase in contact with the surrounding atmosphere due to the surface enlargement of the free-flowing liquid, leads to an increase in gas content compared to the liquid entering the installation. in the liquid jet leaving the installation and to experience a fresher taste when drinking a drinkable liquid after it has flowed through the installation.
    The experience of more freshness and improved taste can probably be traced back to both the increased gas content and the change in the charge distribution, so that an enhanced stimulation of the taste senses can be imagined. The precise mechanisms of perceiving taste have not been fully explained due to the complexity of the processes. However, as explained above, the demonstrable effects on taste can be explained at least theoretically.
    In principle, it is not excluded that the installation described here for handling liquids from several parts is assembled. However, it is preferable to manufacture the installation in one part, for example by producing the installation by 3D printing or casting it, for example by means of a lost core method.
    In order to be able to ensure the maximum possible axial inflow of liquid into the installation, based on the virtual flow axis of the installation, it is advantageous if the longitudinal center line of the installation, which can be determined as the flow axis, cuts through the inlet opening of the installation. The less the inlet opening deviates from the flow axis, the less is also the momentum or the vortex, which the fluid experiences when it enters the installation. Therefore, it is preferable that the flow axis intersects the inlet opening in the inflow section through the center, so that - conceivably - the virtual flow axis of the installation passes through the center of gravity of the cross-sectional area of the inlet opening.
    In order to be able to collect the liquid flowing out of the installation as freely as possible from losses in a vessel, it is also preferred that the flow axis intersects the outlet opening, preferably intersects the outlet opening in the middle.
    The inflow opening is preferably located at an axial distance from the entrance of the spiral channel. In this way, as much as possible axial inflow of the spiral channel is ensured.
    Although it is possible for the invention described here that the outflow opening is located directly at the end of the spiral channel, this is not the only possible location for placing the outflow opening. The effect described above of atomization charge distribution and surface enlargement for the purpose of receiving a larger quantity of gas can also be achieved if a diffuser section is placed axially between the outflow opening and the spiral channel, which diffuser preferably connects axially to the spiral section, the flow-through area of the diffuser section along the flow axis in the direction from inflow opening to outflow opening becomes larger, preferably evenly larger. Due to this increase - from the surface of the cross-section - in the direction from the inflow opening to the outflow opening, the diffuser section for the liquid flowing out of the spiral channel allows an expansion and thus a surface enlargement, the diffuser section also spraying excessively around the liquid emerging from the spiral channel. The use value of the invention increases as a result, because the diffuser section simplifies the collection of the emerging liquid in a collection vessel.
    In essence, the diffuser section can be placed in any direction. Preferably, however, the diffuser section will be axially oriented with respect to the flow direction. The diffuser section can even be constructed symmetrically or in particular rotationally symmetrically based on the flow axis. In these cases, the orientation of the angle of the installation relative to the virtual flow axis is not important. Because in this invention the virtual flow axis runs coaxially with the axis of the fluid line from which the fluid is led into the processing unit, it certainly does not affect the angle at which the installation runs with an axially extending, in particular with a rotationally symmetrical, diffuser section. connected to or connected to the pipeline.
    For the rest, it is preferred for this reason to construct the inflow section exclusively axially, preferably symmetrically, in particular rotationally symmetrically with the flow axis as the axis of symmetry.
    To further improve the operation of the installation, a concentration section can be placed axially between the diffuser section and the outflow opening, which concentration section preferably connects axially to the diffuser section and which preferably forms the outflow opening, the flowable surface of the concentration section along the flow axis in the direction of the outflow opening becomes smaller, preferably evenly smaller.
    The concentration section, which preferably runs exclusively axially and which rejuvenates along the flow axis in the direction of the outflow opening, can result in an additional post-acceleration after flowing through the diffuser section, which is the case at the outflow opening, which preferably at the outflow opening. end of the concentration section remote from the spiral channel leads to a stretched charge-separating atomization around the liquid jet, again with an enlarged surface, flowing out freely from the outflow opening.
    Both a simplified attachment of the installation to the liquid-supplying liquid line and a simplification of the collection of the outflowed liquid after it has flowed through the concentration section can be achieved in that the concentration section is only axially, preferably symmetrical, in particular rotationally symmetrical with the flow axis as a symmetry axis.
    The preferably exclusively axial orientation of the flow-through spaces of the inflow section, the diffuser section and the concentration section, also serves to avoid flow losses and hence undesired turbulences in the liquid flowing through the installation.
    An axially shortest installation, which only extends the fluid line to which it is connected or can be connected in the axial direction, can be achieved in that the inflow opening and / or the outflow opening has / have an opening surface (s) that is orthogonal to the direction of flow. stand.
    To attach the installation to a liquid line, the inflow section can have a fixing part with a connection, which preferably allows a positive mechanical closure to the liquid line. Such a positive mechanical connection is also resistant to higher reaction forces that may result from the liquid flowing through. Tested are fastening parts with closures such as a screw thread, preferably an internal screw thread, in order to enable, in conjunction with an external screw thread on the liquid line, simple screwing and unscrewing of the installation on this pipe. Preferably, the installation can be connected in this way to a tap, such as a water tap. For the purpose of the functionality of the installation, the inflow section is preferably carried out rotationally symmetrically; this preference does not necessarily apply to the connection of the fixing part. This can alternatively also be designed as a bayonet fitting.
    Preferably the carrier of the mounting part but not the mounting part itself has a symmetrical, preferably rotationally symmetrical, shape, with the flow axis as the axis of symmetry.
    In principle, it is preferred that the installation, at least the inflow section and the spiral channel, is made of a solid material. Due to the possibility of simplified design, this material can be a deformable plastic. The diffuser section and the concentration section can also - if available - be made from such a solid material.
    For parts of the installation, in particular for the radially outward facing walls, which limit the flow space of the installation from the inside radially outwards, materials with meshes such as, for example, wire mesh, plastic mesh, fabrics, knotted fabrics and similar, cannot be excluded. to become. The sieve-like structure of these materials leads to a reduction in the mass of the installation and also allows additional absorption of gas by the liquid flowing through it during the flow of the installation. Preferably, the diffuser section and the concentration section - if any - are made from such meshed materials. By constructing at least a part of the flow-through space of the installation from such a material with meshes, in particular in the vicinity of the outlet of the installation, the existing tangential velocity component of the flowing-through liquid can be somewhat reduced with which excessive disintegration or spraying of the free-flowing liquid can be limited or completely prevented.
    In order to guide the inflowing liquid into the installation with as little swirl as possible, it is preferable that the flowable space of the spiral channel is described with an outer cone radially enveloping this channel. This cone is described by a cone, wherein the flow axis describes the axis of the cone and wherein the apex angle between the cone axis and the wall of the cone is between 4 ° and 30 °, preferably between 4 ° and 10 ° , in particular between 4 ° and 8 °.
    Opposite this outer cone can be a virtual inscribed inner cone around which the flowable space of the spiral channel runs radially. This inner cone can again be described as a cone with the flow axis as the axis of the cone, the apex angle between the cone axis and the wall of the cone being between 0.1 ° and 15 °, preferably between 0 , 2 ° and 1.5 ° in particular between 0.2 ° and 0.8 °.
    The two described cones, the enveloping cone and the inscribed cone, describe a virtual enclosure, the walls of which abut tangentially, radially outside and radially inside, respectively, against the flow-through space of the spiral channel.
    In order to guarantee a flow path necessary for the desired acceleration, the installation can further be designed such that a tangent to the spiral, which is described by the geometric location of the centers of gravity of the cross-sectional area, which the flowable space of the intersect the spiral section orthogonally with respect to the flow direction, considered in radial direction of the flow axis with this flow axis making an angle lying between 30 ° and 80 °, preferably between 50 ° and 60 °.
    Preferably, the described angle between the flow axis and the surface of the cross-sections of the flow-through space of the spiral section is constant at least for a central part of the spiral section. The central part of the spiral section is understood to mean an axial segment of the spiral section, without inflow part or outflow part, which are required to guide the axial inflowing liquid into a spiral flow or to guide the spiral flow into an axial outflow. The spiral section thus has a constant slope, with the axial pitch decreasing with the flowed length per rotation about the flow axis, because namely the surface of the flowed section of the flowable space in the spiral section decreases along the flow axis in the direction of the outflow opening.
    In the following, further aspects of potentially valuable variants of the present invention are described.
    In order to avoid flow losses, the spiral flow-through space of the spiral section is preferably free of corners and edges both in the flow direction and in the circumferential direction about the spiral flow through the spiral section. The spiral channel can therefore be described by a wall that is curved about two axes. The one axis of curvature is formed by an axis that runs parallel to the axis of the flow or is that flow axis itself. The other axis of curvature is described by a local tangent to the coil describing the channel.
    Thus, when the flow axis is one of the descriptive axes of the intersecting surface, longitudinal sections of the flowable space of the spiral channel will preferably be oval or circular. At the location of the opening where the liquid flows into the spiral channel and at the location of the opening where the liquid leaves the spiral channel, the shape of these longitudinal sections may deviate from a pure circle or oval shape.
    The cross-sectional area of the flow-through space of the spiral channel decreases by 10% to 40% per winding of the spiral, always based on the larger surface of two axially adjacent cross-sections. This decrease is preferably from 22% to 37%, in particular from 22% to 32%.
    Preferably, the decrease in cross-sectional area through the flowable space of the spiral channel is degressive. That is, the percentage reduction in the cross-sectional area decreases in the direction from the inlet opening to the outlet opening, preferably decreases uniformly.
    The liquid flow flowing through the installation is preferably not shared during the flow of the installation. That is, the liquid enters the plant as a single or single jet, this jet flows through the plant as a single undivided stream and leaves the plant as a single liquid jet.
    Preferably, water is processed with the present fluid processing plant. However, apart from water, any other liquid can be passed through the processing plant. For example, it is conceivable that flammable liquids, in particular motor fuels, are passed through the installation in particular to increase the content of the oxygen dissolved in the fuel in order to increase the energy yield from this fuel that is available per unit of time.
    The present invention will be described in more detail below with reference to the accompanying drawings. The figures show the following:
    Figure 1 A perspective view of an embodiment of the invention of a processing unit for flowing liquids.
    Figure 2 A longitudinal section through the same embodiment.
    Figure 3 An enlarged longitudinal section of the spiral channel of the flowing fluid processing unit of Figures 1 and 2.
    In figures 1 and 2 the invention described in this document for a processing unit for flowing liquids is generally indicated by 10. The installation extends along the virtual flow axis S, which forms a longitudinal axis, from the end where the liquid flows into the installation 10a to the end where the liquid leaves the installation 10b.
    The virtual flow axis S herein defines a coordinate system, wherein the direction of the flow axis is indicated in the present description as an axial direction, the direction perpendicular to the flow axis S is referred to as a radial direction and the direction on a cylinder which is located around the flow axis when circumferential direction is indicated.
    At the inlet-side axial end 10a of the processing unit 10 there is an inflow section 12 to which a spiral section 14 connects axially.
    Axially on the outlet side 10b of the processing unit 10 there may be a diffuser section 16 and a subsequent concentration section 18 axially.
    Liquid flows axially into the installation 10 on the inlet side 10a (see arrow 20).
    The liquid 20 may, for example, be water which is delivered axially to the processing unit by a tap or tap point (not shown in Figs. 1 to 3).
    To connect the installation to a water pipe or to a liquid pipe in a general sense, the processing unit 10, more specifically the inlet section 12, may be provided with a fastening part with connection 22, for example in the form of an internal thread, with which the installation supplies liquid to fix the pipe, in particular to screw it down.
    In essence, the liquid flows axially through the entrance opening 24 into the inlet section 12. The inlet opening 24 can be provided with a radially inwardly offset axial stopper 26a. This stopper serves for relative axial positioning of the installation 10 on the liquid line with which the installation 10 at the end on the entrance side 10a is connected to or connected to the liquid line.
    Preferably, the cross-sectional area of the inflow opening 24 is orthogonal to the flow axis S. And, preferably, the flow axis S intersects the center of the surface. In the present example, the inflow opening is essentially circular, so that the flow axis S passes through the center of the circle that forms the inflow opening 24.
    After passage through the inflow opening 24, the liquid jet or the liquid flow, respectively, enters the spiral section 14, where a flowable space 28 spirals around the flow axis S. The described example shows a spiral section with four turns 30 to 36. The number of windings here merely serves as an example. The actual installation can actually have more than four or fewer than four turns. However, four turns are sufficient to achieve the results intended by the invention without the installation being too large in the axial direction.
    The cross-sectional area of the spiral channel 28 of spiral section 14 decreases uniformly from turn to turn. Since liquids are generally non-compressible, this means that the initially axially inflowing liquid is deflected in a spiral flow and then accelerated uniformly along the flow path of the spiral channel 14, because the decrease in the surface area of the cross-section of the flow-through space 28 along the spiral section about the flow axis S preferably runs steadily and uniformly.
    Furthermore, the radial distance from the flowable space 28 to the flow axis S from winding to winding from the inflow side longitudinal end 10a to the outflow side longitudinal end 10b becomes increasingly smaller, preferably evenly smaller, so that the inflowable spiral space 28 in essentially describes a conical envelope on the spiral section 14. As a result of this reduction of the radius during axial advancement along the flow axis S, the liquid flowing through the spiral section 14 is accelerated not only uniformly in the flow direction, but also orthogonal to this direction, i.e. centripetal.
    In Fig. 3 an outer outer cone 38 is indicated which, viewed in longitudinal section, tangentially touches the outside of the flow-through space 28 with the longitudinal section of the cone-describing line 40. This enveloping cone 38 describes a cone angle between the wall of the cone 40 and the axis of the cone coinciding with the flow axis S. The magnitude of this angle is of the order of 4 ° to 30 ° and is approximately 7 ° in the example.
    Similarly, the flow-through space 28 of the spiral section 14 describes an inscribed cone 42, the cone of which is described by a tangent 44 located in the cutting plane and tangent to the inside of the flow-through space 28 of the spiral section. This tangent-describing tangent 44 describes, with the axis of the cone coinciding with the flow axis S, a cone angle β of the inscribed cone 42. The magnitude of this angle is of the order of 0.Γ to 15 ° and is in the example about 1.9 °.
    The above-described cones from Figure 3 are partly established as the cross-sectional area of the flowable spiral space 28 across the spiral from winding to winding decreases in the direction from the inflow opening to the outflow opening.
    For example, in Figure 3, the cross-sectional area 34a opposite the cross-sectional area 32a, which in the same longitudinal section is downstream, decreases by approximately 30% (based on the larger surface area 32a).
    The surface of cross-section 36a of the flow-through space of the spiral channel 28 is also in the same longitudinal section and decreases by about 24% opposite the surface of a winding upstream section 34a.
    The edges of the walls of the steamable space 28 are curved in the considered longitudinal section and free of corners and edges. Preferably, the cross-sectional area of the spiral flow-through space 28 in the illustrated longitudinal section is oval in shape or circular.
    A consideration of cross-sections that are orthogonal to the flow axis S also shows that the flowable space 28 of the spiral section 14 advantageously has no edges or corners, but is curved with a radius of curvature decreasing in the direction of the outflow opening .
    A tangent 46 at the centerline of the flow-through space, which is geometrically determined by the centers of gravity of all cross-sections of the flow-through space 28, describes, when projecting this tangent in radial direction to the flow axis S, with this flow -as S an angle γ, which is between 30 ° and 80 °. In the example, the size of this angle is approximately 58 °. The angle γ preferably remains substantially constant over the entire spiral section.
    After the liquid has flowed through the spiral section 14, the liquid can flow into a diffuser section 16 which is located along the flow axis S towards the outflow opening 48. After the acceleration in the spiral section 14, the liquid in the diffuser section 16 can expand abruptly. A diffusion section 18 can be connected axially to the diffuser section 16, along which the liquid coming from the spiral section 14 can be guided again in an axial flow direction.
    The concentration section may consist of a shape rejuvenating along the flow axis in the direction of the outflow opening 48, so that the liquid flowing through it will be accelerated again. Figure 2, however, does not depict a conical or otherwise rejuvenating concentration section in the direction of the outflow opening 48. Dotted lines, however, indicate a rejuvenating alternative to the concentration section.
    When flowing out of the outflow opening 48, which is preferably oriented orthogonally to the flow axis, that is to say the cross-sectional area is orthogonal to the flow axis S, and which is preferably circular, wherein - just like at the inflow opening 24 - the flow axis S passes through the center of the circle, the fluid flows axially as a free radius, so that also the outflowing fluid jet is essentially central and symmetrical, in particular rotationally symmetrical, around the flow axis S if symmetry axis can flow out. Radially around the outflowing liquid jet, due to the strong accelerations that act on the liquid during the flow through of the processing unit 10, strong atomization or formation of droplets of a size in the sub-micrometer domain results in charge separation. Although the number of charge carriers on leaving the processing unit 10 is equal to the number on entering the processing unit 10, they are distributed differently, that is to say inhomogeneously, after leaving the outflow opening 48. Measurements around the outflowing liquid jet show that charge with an electrical polarity concentrates in the environment of the free-flowing liquid jet, while charge with the opposite polarity concentrates in the jet itself.
    In addition, the free liquid jet flowing out of the outflow opening 48 has such a large surface area that is in contact with the atmosphere surrounding it that the liquid flowing out in this jet absorbs above average amount of gas in a short time, and thus within a short distance, which can lead to a sharp increase in the amount of oxygen absorbed in the liquid.
    The enrichment of the liquid with gas, in particular with oxygen, in combination with the charge separation - which, incidentally, can also be observed with waterfalls - with water, among other things, leads to a substantial improvement in taste compared to raw water produced from the same guidance comes from. This improvement can theoretically be explained by the enrichment with oxygen and by the possibility that the charge concentration brought about by the charge separation in the liquid facilitates the activation of the taste buds and the associated nerves.
    权利要求:
    Claims (12)
    [1]
    A flowing fluid processing unit (10) which extends around a virtual flow axis (S) which is also the longitudinal axis of the processing device and which is composed of: - an inflow section (12), which for inflowing the liquid in the installation is connected to or connectable to a liquid line running around the axis of a line (at S), wherein the inflow section has an inflow opening (24) through which liquid can flow into the processing unit, - a, related to the flow axis (S), flowable spiral section connecting axially to the inflow section (12), the flowable space of which (28) runs spirally around the flow axis (S), - an outflow opening (48) axially following the spiral section through which fluid flowing out of the plant, characterized in that the inflow section (12) is constructed such that the flow axis (S) of the plant is coaxial with the axis of the fluid line, is connected or will be connectable, and that the surface flow through the liquid (32a, 34a, 36a) of the spiral steamable space (28) of the spiral section (14) decreases along the flow axis (S) in the direction of the inflow opening (24) to the outflow opening (48).
    [2]
    An installation (10) for processing a liquid flowing through it as in claim 1, characterized in that the flow axis (S) cuts through the inflow opening (24), preferably cuts through the middle.
    [3]
    A processing unit for flowing liquids (10) as in claim 1 or 2, characterized in that the flow axis (S) cuts through the outflow opening (48), preferably cuts through the middle.
    [4]
    A flow-through liquid processing unit (10) as mentioned in any one of the preceding claims, characterized in that a diffuser section (16) is located axially between the spiral section (14) and the outflow opening (48), which is preferably axially on the spiral section (14), wherein the flowable area of the cross-section of the diffuser section (16) along the flow axis (S) in the direction from the inflow opening (24) to the outflow opening (48) becomes larger, preferably evenly larger.
    [5]
    A processing unit for flowing liquids (10) as in claim 4, characterized in that the diffuser section (16) runs exclusively axially and / or is constructed symmetrically, preferably rotationally symmetrically, with the flow axis (S) as the axis of symmetry.
    [6]
    A flowing fluid processing unit (10) as in claim 4 or 5, characterized in that a concentration section (18) is located axially between the diffuser section (16) and the outflow opening (48), which is preferably axially on the diffuser section (16). ) and which particularly preferably forms the outflow opening (48), the flowable surface of the section of the concentration section (18) along the flow axis (S) in the direction from the inflow opening (24) to the outflow opening (48) becomes smaller, preferably evenly smaller.
    [7]
    A processing unit for flowing liquids (10) as mentioned in one of the preceding claims, characterized in that the opening surface or the opening surfaces of the inlet opening (24) and / or the outlet opening (48) are orthogonal to the flow axis (S) ) is or are constructed.
    [8]
    A processing unit for flowing liquids (10) as mentioned in one of the preceding claims, characterized in that the inflow section (12) is provided with a fastening part (22) with connection, preferably a screw thread, in particular an inner thread - screw thread, for attaching the installation (10) to a liquid line, in particular a tap, for example a water tap.
    [9]
    A flow-through liquid processing unit (10) as mentioned in any one of the preceding claims, characterized in that the flow-through space (28) of the spiral section (14) has an outer cone (38) surrounding this radially enveloping, with the flow axis (S) as a cone axis and an opening angle (a) between the cone wall (40) and cone axis which are between 4 ° and 30 °, in particular between 4 ° and 10 °, preferably between 4 ° and 8 °.
    [10]
    A flow-through liquid processing unit (10) as mentioned in any one of the preceding claims, characterized in that the flow-through space (28) of the spiral section (14) runs around a radially inwardly written cone (42), with the flow axis (S) as a cone axis and an opening angle (β) between the cone wall (44) and the cone axis which is between 0.1 ° and 15 °, preferably between 0.2 ° and 1.5 °, in particular between 0.2 ° and 0.8 °.
    [11]
    A flowing fluid processing unit (10) as mentioned in any one of the preceding claims, characterized in that a tangent (46) on the center line of the flowable space, which center line is geometrically determined by the centers of gravity of the surface of the cross sections (32a, 34a, 36a), orthogonal to the local flow direction, from the flowable space (28), when projecting this tangent in radial direction to the flow axis (S), with this flow axis (S) angled (γ), which is between 30 ° and 80 °, preferably between 50 ° and 60 °.
    [12]
    A processing unit for flowing liquids (10) as mentioned in any one of the preceding claims, characterized in that it is partly or entirely made of a material with meshes, such as mesh, braid or knotted material and similar material.
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